WO2010021053A1 - Mercury removing system for equipment for carbon dioxide recovery from combustion exhaust gas and method of mercury removing operation for equipment for carbon dioxide recovery from combustion exhaust gas - Google Patents

Mercury removing system for equipment for carbon dioxide recovery from combustion exhaust gas and method of mercury removing operation for equipment for carbon dioxide recovery from combustion exhaust gas Download PDF

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Publication number
WO2010021053A1
WO2010021053A1 PCT/JP2008/064968 JP2008064968W WO2010021053A1 WO 2010021053 A1 WO2010021053 A1 WO 2010021053A1 JP 2008064968 W JP2008064968 W JP 2008064968W WO 2010021053 A1 WO2010021053 A1 WO 2010021053A1
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Prior art keywords
mercury
exhaust gas
combustion exhaust
gas
carbon dioxide
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PCT/JP2008/064968
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French (fr)
Japanese (ja)
Inventor
久幸 折田
向出　正明
穂刈　信幸
強 柴田
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株式会社日立製作所
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Priority to PCT/JP2008/064968 priority Critical patent/WO2010021053A1/en
Priority to JP2010525538A priority patent/JP5253509B2/en
Publication of WO2010021053A1 publication Critical patent/WO2010021053A1/en

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/50—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/60—Heavy metals; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/60—Sorption with dry devices, e.g. beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/15061—Deep cooling or freezing of flue gas rich of CO2 to deliver CO2-free emissions, or to deliver liquid CO2

Definitions

  • the present invention relates to a mercury removal system in a carbon dioxide recovery facility in combustion exhaust gas and a mercury removal operation method of the carbon dioxide recovery facility in combustion exhaust gas.
  • the “Summary of Report on Mercury Effects Investigation Committee” in the technical literature states that when LPG is vaporized, the gas temperature becomes low, and mercury in the vaporized LPG liquefies and accumulates. It is disclosed that in order to prevent the member from corroding and further to prevent the metal member from corroding, it is necessary to manage in advance to reduce the mercury concentration in the LPG.
  • LPG As a method for reducing the mercury concentration in LPG, for example, in Japanese Patent Application Laid-Open No. 9-221684, LPG is supplied into a packed bed of mercury adsorbent, and the mercury adsorbent is used under adsorption conditions at a temperature of 20 ° C. to 200 ° C. A technique for removing mercury by bringing it into contact with water is disclosed.
  • CO 2 carbon dioxide
  • the thermal power plant is attracting attention as a CO 2 emission source, and it is desired to separate and remove CO 2 in the combustion exhaust gas discharged from the boiler of the thermal power plant with high efficiency.
  • Japanese Patent No. 3068888 discloses a technique for increasing the concentration of CO 2 by burning fuel and oxygen in a boiler.
  • Hg 0 metallic mercury
  • HgCl 2 A technique for converting to mercury chloride (hereinafter referred to as HgCl 2 ) which is easily dissolved and absorbing it in water and removing it, and a technique for removing this HgCl 2 by absorbing it in an adsorbent are disclosed.
  • Japanese Patent Laid-Open No. 9-221684 Japanese Patent No. 3068888 JP 2004-237244 A JP 2005-230810 A Summary of the Mercury Effects Investigation Committee Report (Ministry of Economy, Trade and Industry, NISA, High Pressure Gas Safety Association, March 29, 2002)
  • the total amount of HgCl 2 may be removed by dissolving in water. However, it is difficult to convert the entire amount of Hg 0 to HgCl 2 , and a part of Hg 0 remains.
  • An object of the present invention is to collect CO 2 from combustion exhaust gas and to remove Hg 0 contained in the combustion exhaust gas with high accuracy, and to remove mercury from the carbon dioxide recovery facility in the combustion exhaust gas, Another object is to provide a mercury removal operation method for carbon dioxide recovery equipment in combustion exhaust gas.
  • the mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas includes a dehydrator for removing moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas, and a dehydrator installed downstream of the dehydrator.
  • a plurality of mercury gas adsorption towers for adsorbing and removing mercury in combustion exhaust gas are arranged in parallel between the dehydrator and the compressor.
  • the mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas is installed on the downstream side of the dehydration device for removing moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas.
  • a compressor that compresses carbon dioxide in the flue gas from which moisture has been removed, and a carbon dioxide recovery facility in the flue gas that has a cooler that cools and liquefies the compressed carbon dioxide, and upstream of the dehydrator Alternatively, a plurality of mercury gas adsorption towers that adsorb and remove mercury in combustion exhaust gas are arranged in parallel between the dehydrator and the compressor, and a plurality of mercury gas adsorption towers arranged in plurality are arranged.
  • An inlet valve and an outlet valve for adjusting the flow of combustion exhaust gas are installed on the upstream side and the downstream side, respectively, and a mercury analyzer for measuring the mercury concentration in the combustion exhaust gas is installed on the downstream side of the outlet valve. Based on the concentration of mercury in the combustion exhaust gas measured by the analyzer is characterized in that in which the controllable device for controlling the opening and closing of the inlet valve and outlet valve of the mercury gas adsorption tower.
  • the mercury removal operation method of the carbon dioxide recovery equipment in the combustion exhaust gas of the present invention is a method in which the moisture in the combustion exhaust gas discharged from the source of the combustion exhaust gas is removed by the dehydrator, and the moisture is removed by this dehydrator.
  • the carbon dioxide is compressed by a compressor installed on the downstream side of the dehydrator, and the compressed carbon dioxide is cooled and liquefied by a cooler to recover the carbon dioxide from the combustion exhaust gas.
  • One mercury gas in a mercury gas adsorption tower that adsorbs and removes mercury in combustion exhaust gas arranged upstream in parallel with the dehydrator or between the dehydrator and the compressor.
  • An operation is performed to remove the mercury in the flue gas by ventilating the flue gas before flowing into the dehydrator or the flue gas after flowing down the dehydrator with respect to the adsorption tower.
  • the mercury removal operation method of the carbon dioxide recovery facility in the combustion exhaust gas of the present invention is a combustion in which moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas is removed by the dehydrator, and moisture is removed by this dehydrator.
  • the mercury in the combustion exhaust gas is adsorbed and removed by a mercury gas adsorption tower provided upstream in parallel with the dehydrator or in parallel between the dehydrator and the compressor, the mercury gas adsorption Among the mercury gas adsorption towers installed in parallel based on the mercury concentration in the combustion exhaust gas flowing down the tower, the dehydration device is attached to one mercury gas adsorption tower.
  • the combustion exhaust gas before flowing into the exhaust gas, or the exhaust gas after flowing down the dehydrator is controlled so as to ventilate and the mercury in the combustion exhaust gas is removed and the combustion exhaust gas flowing down the mercury gas adsorption tower
  • the combustion exhaust gas is vented to at least one mercury gas adsorption tower in a standby state without allowing the combustion exhaust gas to pass through the mercury gas adsorption tower. In this way, the combustion exhaust gas is switched so as to be ventilated so as to remove mercury in the combustion exhaust gas.
  • a system for removing mercury from a carbon dioxide recovery facility in combustion exhaust gas which is capable of recovering CO 2 from the combustion exhaust gas and removing Hg 0 contained in the combustion exhaust gas with high accuracy, And the mercury removal operation method of the carbon dioxide recovery equipment in combustion exhaust gas is realizable.
  • FIG. 1 The schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 1st Example of this invention.
  • the schematic diagram which shows an example of the arrangement
  • the schematic diagram which shows the other example of arrangement
  • FIG. 1 The schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 1st Example of this invention.
  • the schematic diagram which shows an example of the arrangement
  • FIG. 3 is a structural diagram showing an example of a heating structure of a metal mercury adsorbent installed inside the metal mercury gas adsorption tower shown in FIG. 2.
  • the schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 2nd Example of this invention.
  • the schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 3rd Example of this invention.
  • Metal mercury gas adsorption tower used in the mercury removal system according to the first embodiment of the present invention shown in FIG. 1 A diagram showing symbols of the metal mercury gas adsorption tower, inlet valve, outlet valve and mercury analyzer of the present invention. .
  • the flowchart which initializes ventilation control of the combustion exhaust gas with respect to the metal mercury gas adsorption tower used for the mercury removal system which is 1st Example of this invention shown in FIG. The flowchart which shows an example of switching control of the combustion exhaust gas with respect to the metal mercury gas adsorption tower used for the mercury removal system which is 1st Example of this invention shown in FIG.
  • the mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to the first embodiment of the present invention shown in FIG. 1 combusts pulverized coal of fuel together with air to generate high-temperature combustion gas, and this combustion gas Is used as a heat source to generate a high-temperature steam and supply a steam supply destination (not shown) such as a steam turbine.
  • a combustion exhaust gas treatment system for treating combustion exhaust gas discharged from a pulverized coal burning boiler 50 which is a source of combustion exhaust gas that generates combustion exhaust gas by burning fuel and air, is disposed downstream of the pulverized coal burning boiler 50, respectively.
  • the dust collector 1 removes the combustion ash and the desulfurizer 2 that is located downstream of the dust collector 1 and removes sulfur oxide (hereinafter referred to as SOx) in the combustion exhaust gas 21.
  • a dehydration device 3 for removing moisture in the combustion exhaust gas 21 and a downstream side of the dehydration device 3 are installed.
  • a compressor 4 that compresses CO 2 in the combustion exhaust gas from which moisture has been removed, and a cooler 5 ′ that cools and liquefies the CO 2 compressed by the compressor 4 are provided.
  • the water removed from the combustion exhaust gas 21 by the dehydrator 3 is discharged as water 22 from the dehydrator 3 to the outside.
  • Hg 0 contained in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 is stacked inside metal mercury adsorption towers 11 and 11 ′ described later installed between the dehydrator 3 and the compressor 4. It is directly removed from the combustion exhaust gas 21 by adsorbing Hg 0 in the combustion exhaust gas 21 with the metal mercury adsorbent.
  • the CO 2 in the flue gas 21 is liquefied by being cooled by the cooler 5 ′, but the Hg 0 is adsorbed and removed by the compression of the compressor 4 and the cooling of the cooler 5 ′.
  • the CO 2 becomes liquefied CO 2 23 and a non-condensable gas 24 that does not liquefy, and the liquefied CO 2 23 is supplied from the cooler 5 ′ to a storage facility (not shown) for liquefied CO 2.
  • the condensable gas 24 is configured to flow further downstream from the cooler 5 ′ and be discharged to the outside.
  • the combustion of the pulverized coal in the pulverized coal burning boiler 50 performs oxygen combustion suitable for CO 2 recovery, but a part of the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 is burned from the downstream side of the dust collector 1. A part of the combustion exhaust gas 21 is configured to circulate to the pulverized coal burning boiler 50 so as to be supplied to the pulverized coal burning boiler 50 through the exhaust gas circulation line 25.
  • the forms of mercury in the combustion exhaust gas 21 produced and discharged by the pulverized coal burning boiler 50 include metallic mercury Hg 0 and mercury chloride HgCl 2 .
  • Hg 0 is mainly used, and Hg 0 is converted into HgCl 2 by the catalyst placed inside the denitration device 51 that reduces nitrogen oxides installed downstream of the pulverized coal burning boiler 50.
  • the converted HgCl 2 is adsorbed by the combustion ash contained in the combustion exhaust gas 21, and is collected on the downstream side of the denitration device 51. It is removed by the dust device 1. Further, the HgCl 2 can be dissolved in water and removed by a desulfurization device 2 that sprays water installed downstream of the dust collector 1.
  • Hg 0 in the combustion exhaust gas 21 has no adsorptivity to combustion ash and no solubility in water, so when nothing is treated, this Hg 0 flows down to the downstream with the combustion exhaust gas 21 from the smoke outlet. Will be released to the atmosphere.
  • the NOx concentration at the boiler outlet is in the range of 100 ppm to 200 ppm.
  • the denitration device 51 installed on the downstream side of the pulverized coal-fired boiler 50, the most of the combustion exhaust gas treatment system.
  • a chimney (not shown) installed downstream is discharged into the atmosphere.
  • the denitration device 51 installed on the downstream side of the pulverized coal burning boiler 50 becomes unnecessary, or The NOx concentration can be further reduced by the denitration device 51 and discharged from the chimney to the atmosphere.
  • Hg 0 in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 is HgCl. since is discharged to the downstream side without being converted into 2, it is necessary to directly remove the Hg 0 from in the combustion exhaust gas 21.
  • the metal mercury gas adsorption towers 11 and 11 ′ are arranged in parallel between the dehydrator 3 and the compressor 4 to perform combustion. Metal mercury Hg 0 was adsorbed from the exhaust gas 21 and directly removed.
  • an alloy containing nickel (hereinafter referred to as Ni) serving as a metal mercury adsorbent is laminated as a plate adsorbent.
  • the alloy containing Ni used for the metal mercury adsorbent include SUS.
  • the main elements constituting SUS are manganese, nickel, and chromium, and all are transition metals. Since the transition metal combines with Hg 0 to form an amalgam, it is effective as an adsorbent for adsorbing Hg 0 . Even if a transition metal is oxidized, it does not form an amalgam. Therefore, nickel that is preferably not easily oxidized is an effective metal mercury adsorbent.
  • the configuration of the mercury removing device in the mercury removing system of the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment will be further described.
  • Two metal mercury gas adsorption towers 11 and 11 ′ are respectively installed in the flow paths arranged in parallel, and an inlet valve 13 is arranged on the upstream side of one metal mercury gas adsorption tower 11 on the downstream side. Each is provided with an outlet valve 14. Similarly, an inlet valve 13 ′ is provided on the upstream side of the other metal mercury gas adsorption tower 11 ′, and an outlet valve 14 ′ is provided on the downstream side.
  • a control device 12 for controlling the ventilation of the combustion exhaust gas 21 to the metal mercury gas adsorption towers 11 and 11 ′ is installed, and an operation signal from the control device 12 determines the metal mercury gas adsorption towers 11 and 11 ′.
  • the combustion exhaust gas 21 can be switched to one of the metal mercury gas adsorption towers 11 and 11 ′ so as to ventilate or both. Is controlling.
  • Mercury analyzers 15 and 15 ' are installed on the downstream side of the outlet valves 14 and 14' of the metal mercury gas adsorption towers 11 and 11 ', respectively, and the metal mercury gas adsorption towers 11 and 11' are arranged.
  • a mercury analyzer 15b is also installed in the downstream merged flow channel where the parallel flow channels that have been merged join to detect the value of the mercury concentration in the combustion exhaust gas 21 flowing down the merged flow channel. .
  • the detected mercury concentration values of the flue gas 21 measured by the mercury analyzers 15, 15 ′ and 15 b are input to the control device 12, respectively.
  • An operation signal is output based on the comparison with the upper limit value of the mercury concentration set in advance by the apparatus 12, and the inlet valves 13, 13 'and outlet valves 14, 14' of the metal mercury gas adsorption towers 11, 11 'are output.
  • the opening / closing operation is performed, and the combustion exhaust gas 21 is controlled to be ventilated to one or both of the metal mercury gas adsorption towers 11 and 11 ′.
  • the control device 12 continuously monitors the detected value of the mercury concentration of the combustion exhaust gas 21 measured by the mercury analyzers 15, 15 ′, 15 b and is installed, for example, on the downstream side of the one metal mercury gas adsorption tower 11.
  • the detected mercury concentration of the flue gas 21 flowing down the one metal mercury gas adsorption tower 11 by the mercury analyzer 15 is a metal mercury that adsorbs Hg 0 stacked inside the one metal mercury gas adsorption tower 11.
  • the inlet valve 13 and the outlet of one of the metallic mercury gas adsorption towers 11 are detected by an operation signal from the controller 12
  • the valve 14 is closed to stop the operation of the one metal mercury gas adsorption tower 11, and the inlet valve 13 ′ and the outlet valve 14 ′ of the other metal mercury gas adsorption tower 11 ′ are turned on. Operation and 'vented to the other metal mercury gas adsorption tower 11' a flue gas 21 this other metal mercury gas adsorption tower 11 is switched to the operation of the.
  • the other metal mercury gas adsorption tower 11 ′ After switching to the operation of the other metal mercury gas adsorption tower 11 ′, the other metal mercury gas adsorption tower 11 ′ is performed by a mercury analyzer 15 ′ installed on the downstream side of the other metal mercury gas adsorption tower 11 ′. The mercury concentration value in the flue gas 21 flowing down is detected and monitored.
  • the upper limit value of the mercury concentration in the combustion exhaust gas 21 set in the control device 12 is a metal member used in the compressor 4 installed on the downstream side of the metal mercury gas adsorption towers 11, 11 ′. Is set based on the mercury concentration in the combustion exhaust gas 21 that can be tolerated.
  • the combustion exhaust gas 21 is changed from ventilation to one metal mercury gas adsorption tower 11 to ventilation to the other metal mercury gas adsorption tower 11 ′, so that the other metal mercury gas adsorption tower 11 ′ is operated independently. While the one metal mercury gas adsorption tower 11 is switched off, the one metal mercury gas adsorption tower 11 removes the metal mercury adsorbent with reduced adsorption performance stacked inside the adsorption tower. Replace with a new metal mercury adsorbent and put it on standby.
  • the other metal mercury gas adsorption tower 11 ′ is operated alone, and the other metal mercury gas adsorption tower 11 ′ is installed by a mercury analyzer 15 ′ installed downstream of the other metal mercury gas adsorption tower 11 ′.
  • the detection value of the mercury concentration of the combustion exhaust gas 21 flowing down the gas has a predetermined mercury concentration by reducing the adsorption performance of the metal mercury adsorbent that adsorbs Hg 0 stacked inside the other metal mercury gas adsorption tower 11 ′.
  • the inlet valve 13 and the outlet valve 14 of one of the metal mercury gas adsorption towers 11 in the standby state are opened by the operation signal from the control device 12, Combustion exhaust gas 21 is temporarily vented to both the other metal mercury gas adsorption tower 11 ′ and the one metal mercury gas adsorption tower 11 so that the other metal mercury gas adsorption tower 11 ′ and one metal mercury gas adsorption tower 11 ′ It is operated both metal mercury gas adsorption tower 11.
  • the metal mercury gas adsorption is performed by the mercury analyzer 15b installed in the downstream merge channel where the parallel channels merge.
  • Mercury concentration value in the flue gas 21 flowing down this merged flow path from both the towers 11 and 11 ′ is detected and monitored, and the mercury in the flue gas 21 is detected by both the metal mercury gas adsorption towers 11 and 11 ′.
  • the concentration is reduced to suppress an increase in the mercury concentration in the combustion exhaust gas 21 due to the operation switching between the one metal mercury gas adsorption tower 11 and the other metal mercury gas adsorption tower 11 ′.
  • the tower 11 is a mercury analyzer 15b installed in the confluence channel on the downstream side of 11 ′, and captures a sudden rise in the mercury concentration in the combustion exhaust gas 21 flowing down the confluence channel, and is applied to the metal mercury gas adsorption tower 11.
  • the parallel operation in which both the metal mercury gas adsorption towers 11 and 11 ′ are operated by aeration of the combustion exhaust gas 21 to the other metal mercury gas adsorption tower 11 ′ on standby. Then, an operation for reducing mercury in which the mercury concentration in the combustion exhaust gas 21 has rapidly increased is performed.
  • the recovery of CO 2 in the combustion exhaust gas 21 in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment is performed by cooling the CO 2 pressurized by the compressor 4 with the cooler 5 ′ and liquefying it. and 2 23, the 'from to perform the recovery of CO 2 23, which is liquefied, non-condensable gas 24 of the combustion exhaust gas 21 which is not liquefied is the cooler 5' cooler 5 separated from the CO 2 23 liquefied by And let it flow down downstream.
  • FIG. 2 is a plate that is a metal mercury adsorbent installed in the metal mercury gas adsorption towers 11 and 11 ′ constituting the mercury removal system in the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment shown in FIG.
  • a specific example of the adsorbent 31 is shown.
  • the plate-like adsorbent 31 constituting the metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 is along the flow direction of the combustion exhaust gas 21 flowing into the metal mercury gas adsorption towers 11, 11 ′.
  • a plurality of layers are stacked so as to form a flow path 21a through which the flue gas 21 flows down between adjacent plate-like adsorbents 31.
  • the metal mercury adsorbent may be used as particles, and the particles may be filled in the metal mercury gas adsorption towers 11 and 11 '. A 31-layer structure was adopted.
  • the plate-shaped adsorbent 31 is replaced by removing the upper surfaces of the metal mercury adsorption towers 11 and 11 ′ or the side surface where the combustion exhaust gas 21 flows out, and replacing the plate-shaped adsorbent 31 with reduced adsorption performance one by one.
  • the plate-like adsorbent 31 may be exchanged, or the plate-like adsorbent 31 may be installed in a mold that can be stacked and replaced with a new plate-like adsorbent 31 together with the mold.
  • FIG. 3 is a plate that is a metal mercury adsorbent installed inside the metal mercury gas adsorption towers 11 and 11 ′ constituting the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment shown in FIG. Another specific example of the adsorbent 31 is shown.
  • the honeycomb adsorbent 32 constituting the metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 has a large number of holes 21b for flowing the combustion exhaust gas 21 along the flow direction of the combustion exhaust gas. It has a formed structure.
  • the honeycomb cam structure can make the adsorption area for adsorbing Hg 0 wider than the laminated structure of the plate-like adsorbent.
  • the reaction between nickel and metal mercury used in the metal mercury adsorbent that is, the reaction that generates amalgam has a higher reaction rate as the temperature is higher. However, if the temperature is too high, the amalgam decomposes and releases metal mercury.
  • the metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 has a temperature range suitable for adsorbing metal mercury.
  • good results were obtained when the temperature of the SUS tube ranged from 170 ° C to 370 ° C.
  • the adsorbent is desirably used in a temperature range of 170 ° C to 370 ° C.
  • adsorbent 31 is provided with heating means.
  • a plate-like adsorbent 31 constituting a metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 has a structure in which a heater 33 is sandwiched between the plate-like adsorbents 31.
  • the heater 33 is preferably made of a material containing nickel such as nichrome wire.
  • the space formed in the plate-like adsorbent 31 in which the heater 33 is installed does not need to be sealed, and the manufacture is simplified.
  • Plate adsorbent 31 adsorb performance is metallic mercury adsorbent reduction of Hg 0 in the combustion exhaust gas 21 used for a long time, the heating in a separate location from the mercury removal system of the combustion exhaust gas of the present embodiment It can be reused as a metal mercury adsorbent by reprocessing.
  • the mercury removal system for carbon dioxide recovery equipment in the combustion exhaust gas of the second embodiment shown in FIG. 5 has the same basic configuration as the mercury removal system in the combustion exhaust gas of the previous embodiment shown in FIG. Therefore, the description of the configuration common to both is omitted, and only the different configuration will be described below.
  • the desulfurization device 2 for removing SOx in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 Between the dehydrator 3 for removing moisture in the combustion exhaust gas 21, metal mercury adsorption towers 11, 11 ′ in which a metal mercury adsorbent that adsorbs and removes Hg 0 in the combustion exhaust gas 21 is laminated are arranged in parallel.
  • the compressor 4 compresses CO 2 in the combustion exhaust gas 21 on the downstream side of the dehydrator 3 that is the downstream of these metal mercury adsorption towers 11, 11 ′. the compressed CO 2 is liquefied by cooling, the cooler 5 'is in the installed configuration for recovering CO 2 23 liquefied.
  • the compressor 4 pressurized CO 2 is liquefied by cooling by the cooler 5 'in the CO 2
  • the non-condensable gas 24 of the combustion exhaust gas 21 that is not liquefied is separated from the CO 2 23 that has been liquefied by the cooler 5 ′ and is caused to flow downstream.
  • the metal mercury adsorption towers 11 and 11 ′ are arranged in parallel in the high temperature region on the upstream side of the dehydration apparatus 3, and therefore flow into the metal mercury adsorption towers 11 and 11 ′.
  • the temperature of the combustion exhaust gas 21 becomes high, and Hg 0 in the combustion exhaust gas 21 can be adsorbed on the metal mercury adsorbent of the metal mercury adsorption towers 11 and 11 ′ to easily form an amalgam.
  • the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the third embodiment shown in FIG. 6 has the same basic configuration as the mercury removal system in the combustion exhaust gas of the previous embodiment shown in FIG. Therefore, the description of the configuration common to both is omitted, and only the different configuration will be described below.
  • a compressor 4 to liquefy by compressing 2 has become the compressor CO 2 compressed in the 4 and liquefied by cooling, liquefied CO 2 23 is cooler 5 'to recover the installed configuration .
  • the CO 2 recovery in the combustion exhaust gas 21 is performed by liquefying CO 2 pressurized by the compressor 4 by cooling it with the cooler 5 ′. 2 , the non-condensable gas 24 of the combustion exhaust gas 21 that is not liquefied is separated from the CO 2 23 liquefied by the cooler 5 ′ and is caused to flow downstream.
  • the metal mercury adsorption towers 11 and 11 ′ are arranged in parallel in a region where the temperature on the upstream side of the desulfurization apparatus 2 is higher, and therefore flow into the metal mercury adsorption towers 11 and 11 ′.
  • the temperature of the combustion exhaust gas 21 to be further increased, and Hg 0 in the combustion exhaust gas 21 can be adsorbed to the metal mercury adsorbent of the metal mercury adsorption towers 11 and 11 ′ to further easily form the amalgam.
  • the mercury removal system for carbon dioxide recovery equipment in the combustion exhaust gas of the fourth embodiment shown in FIG. 7 has the same basic configuration as the mercury removal system in the combustion exhaust gas of the previous embodiment shown in FIG. Therefore, the description of the configuration common to both is omitted, and only the different configuration will be described below.
  • the dehydrator 3 for removing the moisture in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50, CO 2 in the combustion exhaust gas 21 is placed between the metal mercury adsorption towers 11 and 11 ′ arranged in parallel with a metal mercury adsorbent that adsorbs and removes Hg 0 in the combustion exhaust gas 21.
  • a compressor 4 for compression is installed.
  • a cooler 5 for cooling the combustion exhaust gas 21 flowing down the metal mercury adsorption towers 11 and 11 ′ is provided on the downstream side of the metal mercury adsorption towers 11 and 11 ′ arranged in parallel. 5 'and, the second compressor 4' second compressor 4 on the downstream side of compressing CO 2 in the combustion exhaust gas 21 of liquefying CO 2 compressed in cooled, liquefied CO 2
  • the cooler 5 ′ for recovering 23 is installed.
  • a mercury removal system is configured in a carbon dioxide recovery facility in combustion exhaust gas in which a compressor is provided in two stages of a front stage compressor 4 and a rear stage compressor 4 '.
  • the metal mercury adsorption towers 11 and 11 ′ arranged in parallel for adsorbing and removing Hg 0 in the combustion exhaust gas 21 include the cooler 5 and the second compressor 4 ′ at the subsequent stage. You may make it the structure arrange
  • the optimum installation position of the metal mercury adsorption towers 11 and 11 ′ can be determined from the temperature of the combustion exhaust gas 21.
  • the metal mercury adsorbent that adsorbs and removes Hg 0 stacked inside the metal mercury adsorption towers 11 and 11 ′ improves the adsorption performance of Hg 0 as the temperature of the combustion exhaust gas 21 increases. This is because the adsorption performance is lowered when the temperature becomes higher than the decomposition temperature of the amalgam.
  • the temperature of the combustion exhaust gas 21 flowing down between the cooler 5 and the second compressor 4 ′ in the subsequent stage is lower than the temperature of the combustion exhaust gas 21 flowing down between the compressor 4 in the previous stage and the cooler 5. Therefore, if the temperature of the combustion exhaust gas 21 flowing between the front compressor 4 and the cooler 5 is higher than the decomposition temperature of the amalgam, the cooler 5 and the second compressor 4 ′ of the rear stage.
  • the metal mercury adsorption towers 11 and 11 'arranged in parallel may be provided between the two.
  • the CO 2 in the combustion exhaust gas 21 in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment is recovered by cooling the CO 2 pressurized by the second compressor 4 ′ at the subsequent stage with the cooler 5 ′. Then, the liquefied CO 2 is recovered from the cooler 5 ′, and the non-condensable gas 24 of the combustion exhaust gas 21 that is not liquefied is separated from the CO 2 23 liquefied by the cooler 5 ′ and is caused to flow downstream.
  • the metal mercury adsorption towers 11 and 11 ′ are arranged in parallel in a region where the temperature is increased by pressurization by the compressor 4 in the previous stage.
  • the temperature of the combustion exhaust gas 21 flowing into 'becomes high, and Hg 0 in the combustion exhaust gas 21 can be adsorbed to the metal mercury adsorbent of the metal mercury adsorption towers 11 and 11' to further easily form the amalgam.
  • adsorbs Hg 0 in the combustion exhaust gas 21 are stacked inside the metallic mercury adsorption tower 11, 11 '
  • the formation of amalgam formed by combining transition metals such as Ni constituting the metal mercury adsorbent with Hg 0 is close to saturation, and the adsorption performance of Hg 0 is improved. It will be necessary to replace the metal mercury adsorbent regularly.
  • the metal mercury gas adsorption tower 11 having the metal mercury adsorbent having reduced adsorption performance for adsorbing Hg 0 in the combustion exhaust gas 21,
  • the exhaust gas 21 is ventilated by switching from one of the 11 'to a new metal mercury adsorbent and switching to the other of the other metal mercury gas adsorption towers 11 and 11' waiting.
  • the metal mercury in the inside can be continuously removed with high removal efficiency.
  • the concentration of metallic mercury in the combustion exhaust gas 21 to be treated becomes high, and the processing ability to remove metallic mercury is possible only with the metallic mercury adsorbent provided in the metallic mercury gas adsorption towers 11 and 11 'arranged in parallel. If there is a shortage, in order to increase the treatment capacity to remove metallic mercury, in addition to the working metallic mercury gas adsorption tower, there should be two or more standby metallic mercury gas adsorption towers in advance. If three or more metal mercury gas adsorption towers are provided in the mercury removal system in the carbon dioxide recovery facility for combustion exhaust gas according to this embodiment, the metal mercury concentration in the combustion exhaust gas 21 is arranged in parallel. In addition, it becomes easy to cope with a sudden increase beyond the processing capacity of the two metal mercury gas adsorption towers.
  • FIG. 8 schematically shows a metal mercury gas adsorption tower 11 arranged in parallel in the above-described embodiment of the present invention, and a plurality of metal mercury gases installed in parallel through which the combustion exhaust gas 21 is vented.
  • the adsorption tower 11, the inlet valve 13, the outlet valve 14, and the mercury analyzer 15 are schematically shown as symbols.
  • metal mercury gas adsorption towers 11 are arranged in parallel, and these metal mercury gas adsorption towers 11 are denoted by B 1 to B n .
  • the inlet valve 13 installed on the upstream side is connected to VI 1 to VI n and the outlet valve 14 installed on the downstream side is connected to VO 1.
  • the mercury analyzer 15 located downstream of the outlet valve 14 is denoted by S 1 to S n as VO n . Further, denoted mercury analyzer 15b located in the flow path which is merged with the downstream side of the outlet valve 14 in S e.
  • FIG. 9 is a flowchart showing a method for initializing the state of a metal mercury gas adsorption tower having a configuration in which, for example, three units are installed in parallel in the mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to the above-described embodiment of the present invention. It is.
  • the metal mercury gas adsorption tower 11 is opened and the metal mercury adsorbent is exchanged.
  • each metal mercury gas adsorption tower 11 is divided into three types of ventilation, standby and adsorbent exchange, and the operation state of each metal mercury gas adsorption tower 11 divided into these three types is displayed on the monitor. It is desirable to provide the control device 12 with a function that can be visually confirmed by the control device. By providing the control device 12 with these functions, a plurality of metal mercury gas adsorption towers 11 arranged in parallel can be operated systematically. Can be operated.
  • each metal mercury gas adsorption tower 11 controls the opening and closing of the inlet valve 13 and outlet valve 14 corresponding to each metal mercury gas adsorption tower 11 in the controller 12.
  • the “metal mercury gas adsorption tower 11” is set in “setting of the valve open / close state”.
  • the controller 12 As described above, the function of automatically controlling the opening and closing of the inlet valve 13 and the outlet valve 14 of the metal mercury gas adsorption tower 11 in accordance with the operating state of each metal mercury gas adsorption tower 11 or the function of confirming control, It is desirable that the controller 12 be provided.
  • FIG. 10 is a flowchart showing a method for switching and controlling the operation of the metal mercury gas adsorption tower 11 arranged in parallel in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas according to this embodiment.
  • the upper limit value Cr Hg of the mercury concentration in the combustion exhaust gas 21 preset by the control device 12 for each metal mercury gas adsorption tower 11 is set.
  • the mercury concentration C Hg, i in the combustion exhaust gas 21 flowing down the metal mercury gas adsorption tower 11 is measured by a total 15.
  • the measured value C Hg, i of the mercury concentration in the combustion exhaust gas 21 measured by the total 15 is compared with the upper limit value Cr Hg of the mercury concentration set in step 101 for setting the mercury concentration.
  • the searched metal mercury gas adsorption tower 11 continues to operate. However, since there is no problem, the operation of the metal mercury gas adsorption tower 11 is continued.
  • any one of them is controlled by the control device 12.
  • the adsorption tower 11 may be manually selected.
  • the mercury adsorption tower 11 is vented.
  • the mercury concentration measurement value C Hg, i ⁇ the upper limit value Cr Hg in the mercury concentration comparison in the mercury concentration comparison step 104 which depends on the metal mercury adsorbent.
  • the operation proceeds to the next operation state re-change and valve operation step 107, and the control device 12 performs the metal mercury adsorption.
  • the function of comparing the upper limit value Cr Hg of the mercury concentration in the combustion exhaust gas 21 flowing down each metal mercury adsorption tower 11 with the measured value C Hg, i measured by the mercury analyzer 15, the metal mercury adsorbent It is desirable to provide the control device 12 with a function of notifying that the performance has deteriorated and a function of searching for the metal mercury gas adsorption tower 11 whose metal mercury adsorbent should be replaced.
  • FIG. 11 is a flowchart showing a method for additionally controlling the operation of a plurality of metal mercury gas adsorption towers 11 arranged in parallel to the mercury removal system in the carbon dioxide recovery facility for combustion exhaust gas according to this embodiment.
  • a plurality of mercury concentrations are set in the flow path assembly portion of the combustion exhaust gas 21 on the downstream side of the metallic mercury gas adsorption tower 11 installed by the control device 12.
  • An upper limit value Cr Hg, e of the mercury concentration in the combustion exhaust gas 21 set in advance for the combustion exhaust gas 21 as the whole of the metal mercury gas adsorption tower 11 installed in the base is set.
  • step 203 for measuring the mercury concentration with respect to the plurality of metal mercury gas adsorption towers 11 installed, and a plurality of mercury mercury analyzers 15b provided at the flow path assembly on the downstream side of the plurality of metal mercury gas adsorption towers 11 are used.
  • the mercury concentration C Hg, e in the combustion exhaust gas 21 flowing down the metal mercury gas adsorption tower 11 installed in the base is measured.
  • the process proceeds to the next step 204 for comparing the mercury concentration, and the flow rate collection portion of the metal mercury gas adsorption tower 11 is measured.
  • the measurement value of mercury concentration in combustion exhaust gas 21 measured by the mercury analyzer 15b, C Hg, e, is compared with the upper limit value Cr Hg, e of the mercury concentration set in step 201 for setting the mercury concentration upper limit value. .
  • the mercury concentration comparison step 204 if the relationship of the measured value C Hg, e ⁇ the upper limit value Cr Hg, e of the mercury concentration, a plurality of metal mercury gas adsorption towers 11 installed. Since the measured value C Hg, e of the mercury concentration of the combustion exhaust gas 21 as a whole is within the limit range of the upper limit value Cr Hg, e , the current operation state of the plurality of these metal mercury gas adsorption towers 11 installed is determined. Let it continue.
  • the process returns to the step 203 for measuring the mercury concentration related to the plurality of metal mercury gas adsorption towers 11 installed downstream of the metal mercury gas adsorption tower 11.
  • the measurement of the mercury concentration C Hg, e in the combustion exhaust gas 21 flowing down the metal mercury gas adsorption tower 11 installed in a plurality by the mercury analyzer 15b at the flow path collecting portion on the side is continued.
  • the metal mercury gas flowing through the combustion exhaust gas 21 is used.
  • step 205 in which the operating state is searched for waiting, and a plurality of units are installed by the control device 12.
  • the metal mercury gas adsorption tower 11 in which the set value B j of the operation state is replaced with a new metal mercury adsorbent and is on standby (B j 1) is searched from the metal mercury gas adsorption tower 11.
  • any one of them is controlled by the control device 12.
  • the adsorption tower 11 may be selected manually.
  • the mercury concentration in the combustion exhaust gas 21 as a whole is measured by the mercury analyzer 15b provided in the flow passage assembly on the downstream side of the metal mercury gas adsorption tower 11 installed in plural in this way, thereby the metal mercury gas adsorption.
  • Combustion exhaust gas by adding an operating number of metal mercury gas adsorption towers 11 for adsorbing and removing metal mercury in the combustion exhaust gas 21 according to the mercury concentration as a whole measured at the flow path gathering portion on the downstream side of the tower 11 It is possible to perform an operation of venting 21.
  • CO 2 is recovered from the combustion exhaust gas, and Hg 0 contained in the combustion exhaust gas can be removed with high accuracy.
  • a mercury removal system for carbon recovery equipment and a mercury removal operation method for carbon dioxide recovery equipment in combustion exhaust gas can be realized.
  • the metal mercury in the combustion exhaust gas can be removed with high accuracy, so that the member constituting the compressor that liquefies carbon dioxide in the combustion exhaust gas can be operated for a long time without corrosion. Can do.
  • the present invention is applicable to a mercury removal system in a carbon dioxide recovery facility in combustion exhaust gas and a mercury removal operation method of the carbon dioxide recovery facility in combustion exhaust gas.

Abstract

A mercury removing system for equipment for carbon dioxide recovery from combustion exhaust gas, which equipment includes a dehydrator (3) for removing water contents from the combustion exhaust gas having been emitted from a combustion exhaust gas generating source and, disposed downstream of the dehydrator, a compressor (4) for compressing the carbon dioxide contained in the combustion exhaust gas deprived of water contents and a chiller (5') for chilling the compressed carbon dioxide to thereby liquefy the same. The mercury removing system comprises multiple metallic mercury gas adsorptive columns (11,11') for removing by adsorption the metallic mercury contained in the combustion exhaust gas, disposed in parallel relationship either upstream of the dehydrator (3) or between the dehydrator (3) and the compressor (4).

Description

燃焼排ガス中の二酸化炭素回収設備の水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法Mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, and mercury removal operation method for carbon dioxide recovery equipment in combustion exhaust gas
　本発明は、燃焼排ガス中の二酸化炭素回収設備における水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法に関する。 The present invention relates to a mercury removal system in a carbon dioxide recovery facility in combustion exhaust gas and a mercury removal operation method of the carbon dioxide recovery facility in combustion exhaust gas.
　ＬＰＧ中に含まれる水銀は、ＬＰＧを燃料として使用する内燃機関にＬＰＧを供給する気化器を構成する部材を腐食させるので、気化器の腐食が進行すればこの気化器からＬＰＧが漏洩することになる。 Mercury contained in the LPG corrodes a member constituting a vaporizer that supplies LPG to an internal combustion engine that uses LPG as a fuel. Therefore, if the corrosion of the vaporizer proceeds, the LPG leaks from the vaporizer. Become.
　例えば、技術文献の「水銀影響調査委員会報告書の概要」には、ＬＰＧの気化の際にガス温度が低くなり、気化したＬＰＧ内の水銀が液化、蓄積し、さらに水分の存在下で金属部材が腐食すること、さらに、金属部材の腐食を防ぐために、ＬＰＧ中の水銀濃度を予め削減する管理が必要であることが開示されている。 For example, the “Summary of Report on Mercury Effects Investigation Committee” in the technical literature states that when LPG is vaporized, the gas temperature becomes low, and mercury in the vaporized LPG liquefies and accumulates. It is disclosed that in order to prevent the member from corroding and further to prevent the metal member from corroding, it is necessary to manage in advance to reduce the mercury concentration in the LPG.
　ＬＰＧ内の水銀濃度を削減する方法として、例えば、特開平９－２２１６８４号公報には、水銀吸着剤の充填層内にＬＰＧを供給し、温度２０℃～２００℃の吸着条件下で水銀吸着剤と接触させ、水銀を除去する技術が開示されている。 As a method for reducing the mercury concentration in LPG, for example, in Japanese Patent Application Laid-Open No. 9-221684, LPG is supplied into a packed bed of mercury adsorbent, and the mercury adsorbent is used under adsorption conditions at a temperature of 20 ° C. to 200 ° C. A technique for removing mercury by bringing it into contact with water is disclosed.
　近年、地球温暖化が地球規模の環境問題として取り上げられ、大気中の二酸化炭素（以下、ＣＯ２と記載）濃度の増加が地球温暖化の主要因であることが明らかにされている。 In recent years, global warming has been taken up as a global environmental problem, and it has been clarified that an increase in the concentration of carbon dioxide (hereinafter referred to as CO 2 ) in the atmosphere is the main cause of global warming.
　ところで火力発電所はＣＯ２の排出源として注目されており、火力発電所のボイラから排出される燃焼排ガス中のＣＯ２を高効率で分離、除去することが望まれている。 By the way, the thermal power plant is attracting attention as a CO 2 emission source, and it is desired to separate and remove CO 2 in the combustion exhaust gas discharged from the boiler of the thermal power plant with high efficiency.
　燃焼排ガス中のＣＯ２を高効率で分離、除去するためには、燃焼排ガス中のＣＯ２を高濃度にする必要があるが、ボイラで空気燃焼させた燃焼排ガスは、空気中の約８０ｖｏｌ％を占める窒素によりＣＯ２の高濃度化が抑制される。 In order to separate and remove CO 2 in the combustion exhaust gas with high efficiency, it is necessary to increase the concentration of CO 2 in the combustion exhaust gas, but the combustion exhaust gas burned with a boiler is about 80 vol% in the air. The concentration of CO 2 is suppressed by nitrogen occupying.
　例えば、特許第３０６８８８８号公報には、ボイラで燃料と酸素とを燃焼させることにより、ＣＯ２を高濃度化する技術が開示されている。 For example, Japanese Patent No. 3068888 discloses a technique for increasing the concentration of CO 2 by burning fuel and oxygen in a boiler.
　また、環境問題としてＣＯ２だけでなく、ボイラから排出される燃焼排ガス中の水銀除去が取り上げられている。この燃焼排ガス中の水銀除去の方法として、例えば特開２００４－２３７２４４号公報、および特開２００５－２３０８１０号公報には、燃焼排ガス中の金属水銀（以下Ｈｇ０と表記）を脱硝装置で水に溶解しやすい塩化水銀（以下ＨｇＣｌ２と表記）に変換して水に吸収させて除去する技術、及びこのＨｇＣｌ２を吸着剤に吸収させて除去する技術が開示されている。 Further, as an environmental problem, removal of mercury in combustion exhaust gas discharged from a boiler as well as CO 2 is taken up. As a method for removing mercury in the combustion exhaust gas, for example, in Japanese Patent Application Laid-Open No. 2004-237244 and Japanese Patent Application Laid-Open No. 2005-230810, metallic mercury (hereinafter referred to as Hg 0 ) in the combustion exhaust gas is converted into water by a denitration device. A technique for converting to mercury chloride (hereinafter referred to as HgCl 2 ) which is easily dissolved and absorbing it in water and removing it, and a technique for removing this HgCl 2 by absorbing it in an adsorbent are disclosed.
特開平９－２２１６８４号公報Japanese Patent Laid-Open No. 9-221684 特許第３０６８８８８号公報Japanese Patent No. 3068888 特開２００４－２３７２４４号公報JP 2004-237244 A 特開２００５－２３０８１０号公報JP 2005-230810 A
　燃焼排ガス中のＨｇ０の全量を全てＨｇＣｌ２に変換できれば、ＨｇＣｌ２の全量を水に溶解させて除去すればよい。しかしながら、Ｈｇ０の全量を全てＨｇＣｌ２に変換することは難しく、一部Ｈｇ０が残存する。 If conversion of all the total amount of Hg 0 in the combustion exhaust gas to HgCl 2, the total amount of HgCl 2 may be removed by dissolving in water. However, it is difficult to convert the entire amount of Hg 0 to HgCl 2 , and a part of Hg 0 remains.
　また、燃焼排ガス中からＣＯ２を回収するには、燃焼排ガスを圧縮機で圧縮し、冷却器で圧縮されたＣＯ２を冷却してこのＣＯ２を液化する必要がある。その際に、燃焼排ガス中に含まれているＨｇ０も液化することになるので、前記圧縮機を長時間稼動させているとＨｇ０が圧縮機内に蓄積し、圧縮機を構成する金属部材を腐食させることになる。 Further, in order to recover CO 2 from the combustion exhaust gas, it is necessary to compress the combustion exhaust gas with a compressor, cool the CO 2 compressed with a cooler, and liquefy this CO 2 . At that time, Hg 0 contained in the combustion exhaust gas is also liquefied. Therefore, when the compressor is operated for a long time, Hg 0 accumulates in the compressor, and the metal members constituting the compressor are removed. It will corrode.
　そこで、燃焼排ガス中からＣＯ２を回収する場合に、長時間稼動する圧縮機に供給される燃焼排ガス中のＨｇ０を高精度に除去することが課題となる。 Therefore, when CO 2 is recovered from the combustion exhaust gas, it becomes a problem to remove Hg 0 in the combustion exhaust gas supplied to the compressor operating for a long time with high accuracy.
　本発明の目的は、燃焼排ガス中からＣＯ２を回収すると共に、燃焼排ガス中に含まれたＨｇ０を高精度で除去することを可能にした燃焼排ガス中の二酸化炭素回収設備の水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法を提供することにある。 An object of the present invention is to collect CO 2 from combustion exhaust gas and to remove Hg 0 contained in the combustion exhaust gas with high accuracy, and to remove mercury from the carbon dioxide recovery facility in the combustion exhaust gas, Another object is to provide a mercury removal operation method for carbon dioxide recovery equipment in combustion exhaust gas.
　本発明の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムは、燃焼排ガスの発生源から排出された燃焼排ガス中の水分を除去する脱水装置と、この脱水装置の下流側に設置されて水分を除去した該燃焼排ガス中の二酸化炭素を圧縮する圧縮機及び圧縮された二酸化炭素を冷却して液化する冷却器を有する燃焼排ガス中の二酸化炭素回収設備とを備え、前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に燃焼排ガス中の水銀を吸着して除去する水銀ガス吸着塔を並列に複数基配設したことを特徴とする。 The mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to the present invention includes a dehydrator for removing moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas, and a dehydrator installed downstream of the dehydrator. A compressor for compressing carbon dioxide in the removed combustion exhaust gas, and a carbon dioxide recovery facility in the combustion exhaust gas having a cooler for cooling and liquefying the compressed carbon dioxide, or upstream of the dehydrator, or A plurality of mercury gas adsorption towers for adsorbing and removing mercury in combustion exhaust gas are arranged in parallel between the dehydrator and the compressor.
　また、本発明の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムは、燃焼排ガスの発生源から排出された燃焼排ガス中の水分を除去する脱水装置と、この脱水装置の下流側に設置されて水分を除去した該燃焼排ガス中の二酸化炭素を圧縮する圧縮機及び圧縮された二酸化炭素を冷却して液化する冷却器を有する燃焼排ガス中の二酸化炭素回収設備とを備え、前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に燃焼排ガス中の水銀を吸着して除去する水銀ガス吸着塔を並列に複数基配設し、複数基設配設された各水銀ガス吸着塔の上流側及び下流側に燃焼排ガスの流通を調節する入口バルブ及び出口バルブをそれぞれ設置し、前記出口バルブの下流側に燃焼排ガス中の水銀濃度を計測する水銀分析計を設置し、前記水銀分析計で計測した燃焼排ガス中の水銀濃度に基づいて前記水銀ガス吸着塔の入口バルブ及び出口バルブの開閉を制御する制御装置を設置したことを特徴とする。 In addition, the mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to the present invention is installed on the downstream side of the dehydration device for removing moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas. A compressor that compresses carbon dioxide in the flue gas from which moisture has been removed, and a carbon dioxide recovery facility in the flue gas that has a cooler that cools and liquefies the compressed carbon dioxide, and upstream of the dehydrator Alternatively, a plurality of mercury gas adsorption towers that adsorb and remove mercury in combustion exhaust gas are arranged in parallel between the dehydrator and the compressor, and a plurality of mercury gas adsorption towers arranged in plurality are arranged. An inlet valve and an outlet valve for adjusting the flow of combustion exhaust gas are installed on the upstream side and the downstream side, respectively, and a mercury analyzer for measuring the mercury concentration in the combustion exhaust gas is installed on the downstream side of the outlet valve. Based on the concentration of mercury in the combustion exhaust gas measured by the analyzer is characterized in that in which the controllable device for controlling the opening and closing of the inlet valve and outlet valve of the mercury gas adsorption tower.
　本発明の燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法は、燃焼排ガスの発生源から排出された燃焼排ガス中の水分を脱水装置によって除去し、この脱水装置で水分を除去した燃焼排ガス中の二酸化炭素を該脱水装置の下流側に設置された圧縮機によって圧縮し、圧縮された二酸化炭素を冷却器によって冷却して液化させることによって前記燃焼排ガスからこの二酸化炭素を回収する運転を行い、前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に並列に複数基配設された燃焼排ガス中の水銀を吸着して除去する水銀ガス吸着塔のうち、一基の水銀ガス吸着搭に対して該脱水装置に流入する前の燃焼排ガス、あるいは該脱水装置を流下した後の燃焼排ガスを通気して前記燃焼排ガス中の水銀を除去する運転を行うと共に、前記水銀ガス吸着塔のうち、少なくとも他の１基の水銀ガス吸着搭に対して前記燃焼排ガスを通気させずに待機状態にしておくことを特徴とする。 The mercury removal operation method of the carbon dioxide recovery equipment in the combustion exhaust gas of the present invention is a method in which the moisture in the combustion exhaust gas discharged from the source of the combustion exhaust gas is removed by the dehydrator, and the moisture is removed by this dehydrator. The carbon dioxide is compressed by a compressor installed on the downstream side of the dehydrator, and the compressed carbon dioxide is cooled and liquefied by a cooler to recover the carbon dioxide from the combustion exhaust gas. One mercury gas in a mercury gas adsorption tower that adsorbs and removes mercury in combustion exhaust gas arranged upstream in parallel with the dehydrator or between the dehydrator and the compressor. An operation is performed to remove the mercury in the flue gas by ventilating the flue gas before flowing into the dehydrator or the flue gas after flowing down the dehydrator with respect to the adsorption tower. Both the of mercury gas adsorption tower, wherein the keep the standby state without venting the combustion exhaust gas with respect to the mercury gas adsorption tower of at least one other group.
　また、本発明の燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法は、燃焼排ガスの発生源から排出された燃焼排ガス中の水分を脱水装置によって除去し、この脱水装置で水分を除去した燃焼排ガス中の二酸化炭素を該脱水装置の下流側に設置された圧縮機によって圧縮し、圧縮された二酸化炭素を冷却器によって冷却して液化させることによって前記燃焼排ガスからこの二酸化炭素を回収する運転を行い、前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に並列に複数基設けた水銀ガス吸着塔によって燃焼排ガス中の水銀を吸着させて除去する際に、前記水銀ガス吸着塔を流下した燃焼排ガス中の水銀濃度に基づいてこれらの並列に複数基設設された水銀ガス吸着塔のうち、１基の水銀ガス吸着搭に対して該脱水装置に流入する前の燃焼排ガス、あるいは該脱水装置を流下した後の燃焼排ガスを通気するように制御して前記燃焼排ガス中の水銀を除去する運転を行い、前記水銀ガス吸着塔を流下した燃焼排ガス中の水銀濃度が所定値に達した場合には、前記水銀ガス吸着塔のうち、燃焼排ガスを通気させずに待機状態にある少なくとも１基の水銀ガス吸着搭に対して前記燃焼排ガスを通気させるように燃焼排ガスを切り替えて通気するように制御して前記燃焼排ガス中の水銀を除去する運転を行うことを特徴とする。 Further, the mercury removal operation method of the carbon dioxide recovery facility in the combustion exhaust gas of the present invention is a combustion in which moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas is removed by the dehydrator, and moisture is removed by this dehydrator. An operation of recovering carbon dioxide from the combustion exhaust gas by compressing carbon dioxide in the exhaust gas by a compressor installed on the downstream side of the dehydrator, and cooling the compressed carbon dioxide by a cooler to liquefy it. When the mercury in the combustion exhaust gas is adsorbed and removed by a mercury gas adsorption tower provided upstream in parallel with the dehydrator or in parallel between the dehydrator and the compressor, the mercury gas adsorption Among the mercury gas adsorption towers installed in parallel based on the mercury concentration in the combustion exhaust gas flowing down the tower, the dehydration device is attached to one mercury gas adsorption tower. The combustion exhaust gas before flowing into the exhaust gas, or the exhaust gas after flowing down the dehydrator is controlled so as to ventilate and the mercury in the combustion exhaust gas is removed and the combustion exhaust gas flowing down the mercury gas adsorption tower When the mercury concentration in the chamber reaches a predetermined value, the combustion exhaust gas is vented to at least one mercury gas adsorption tower in a standby state without allowing the combustion exhaust gas to pass through the mercury gas adsorption tower. In this way, the combustion exhaust gas is switched so as to be ventilated so as to remove mercury in the combustion exhaust gas.
　本発明によれば、燃焼排ガス中からＣＯ２を回収すると共に、燃焼排ガス中に含まれたＨｇ０を高精度で除去することを可能にした燃焼排ガス中の二酸化炭素回収設備の水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法が実現できる。 According to the present invention, a system for removing mercury from a carbon dioxide recovery facility in combustion exhaust gas, which is capable of recovering CO 2 from the combustion exhaust gas and removing Hg 0 contained in the combustion exhaust gas with high accuracy, And the mercury removal operation method of the carbon dioxide recovery equipment in combustion exhaust gas is realizable.
本発明の第１実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムを示す概略構成図。BRIEF DESCRIPTION OF THE DRAWINGS The schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 1st Example of this invention. 図１に示した本発明の第１実施例である水銀除去システムに用いられた金属水銀ガス吸着塔の内部に設置される金属水銀吸着剤の配設構造の一例を示す模式図。The schematic diagram which shows an example of the arrangement | positioning structure of the metal mercury adsorption agent installed in the inside of the metal mercury gas adsorption tower used for the mercury removal system which is 1st Example of this invention shown in FIG. 図１に示した本発明の第１実施例である水銀除去システムに用いられた金属水銀ガス吸着塔の内部に設置される金属水銀吸着剤の配設構造の他の例を示す模式図。The schematic diagram which shows the other example of arrangement | positioning structure of the metal mercury adsorption agent installed in the inside of the metal mercury gas adsorption tower used for the mercury removal system which is 1st Example of this invention shown in FIG. 図２に示した金属水銀ガス吸着塔の内部に設置される金属水銀吸着剤の加熱構造の一例を示す構造図。FIG. 3 is a structural diagram showing an example of a heating structure of a metal mercury adsorbent installed inside the metal mercury gas adsorption tower shown in FIG. 2. 本発明の第２実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムを示す概略構成図。The schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 2nd Example of this invention. 本発明の第３実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムを示す概略構成図。The schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 3rd Example of this invention. 本発明の第４実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムを示す概略構成図。The schematic block diagram which shows the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas which is 4th Example of this invention. 図１に示した本発明の第１実施例である水銀除去システムに用いられた金属水銀ガス吸着塔本発明の金属水銀ガス吸着塔、入口バルブ、出口バルブおよび水銀分析計の記号表記を示す図。Metal mercury gas adsorption tower used in the mercury removal system according to the first embodiment of the present invention shown in FIG. 1 A diagram showing symbols of the metal mercury gas adsorption tower, inlet valve, outlet valve and mercury analyzer of the present invention. . 図１に示した本発明の第１実施例である水銀除去システムに用いられた金属水銀ガス吸着塔に対する燃焼排ガスの通気制御を初期設定するフローチャート。The flowchart which initializes ventilation control of the combustion exhaust gas with respect to the metal mercury gas adsorption tower used for the mercury removal system which is 1st Example of this invention shown in FIG. 図１に示した本発明の第１実施例である水銀除去システムに用いられた金属水銀ガス吸着塔に対する燃焼排ガスの切り替え制御の一例を示すフローチャート。The flowchart which shows an example of switching control of the combustion exhaust gas with respect to the metal mercury gas adsorption tower used for the mercury removal system which is 1st Example of this invention shown in FIG. 図１に示した本発明の第１実施例である水銀除去システムに用いられた追加制御される金属水銀ガス吸着塔に対する燃焼排ガスの切り替え制御の一例を示すフローチャート。The flowchart which shows an example of the switching control of the combustion exhaust gas with respect to the metal mercury gas adsorption tower additionally controlled used for the mercury removal system which is 1st Example of this invention shown in FIG.
符号の説明Explanation of symbols
　１：集塵装置、２：脱硫装置、３：脱水装置、４、４’：圧縮機、５、５’：冷却器、１１：金属水銀ガス吸着搭、１２：制御装置、１３：入口バルブ、１４：出口バルブ、１５、１５ｂ：水銀分析計、２１：燃焼排ガス、２２：水（液）、２３：ＣＯ２（液）、２４：非凝縮性ガス、２５：燃焼排ガス循環ライン、３１：板状吸着剤、３２：ハニカム状吸着剤、３３：ヒータ、５０：微粉炭焚きボイラ、５１：脱硝装置。 1: dust collector, 2: desulfurizer, 3: dehydrator, 4, 4 ': compressor, 5, 5': cooler, 11: metal mercury gas adsorption tower, 12: controller, 13: inlet valve, 14: outlet valve, 15, 15b: mercury analyzer, 21: combustion exhaust gas, 22: water (liquid), 23: CO 2 (liquid), 24: non-condensable gas, 25: combustion exhaust gas circulation line, 31: plate 32: honeycomb adsorbent, 33: heater, 50: pulverized coal fired boiler, 51: denitration device.
　本発明の実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運動について図面を用いて説明する。 The mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas and the mercury removal motion of the carbon dioxide recovery facility in the combustion exhaust gas, which are embodiments of the present invention, will be described with reference to the drawings.
　図１を用いて本発明の第１実施例である燃焼排ガス中の二酸化炭素回収の水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法について説明する。 The mercury removal system for carbon dioxide recovery in combustion exhaust gas and the mercury removal operation method for the carbon dioxide recovery equipment in combustion exhaust gas, which are the first embodiment of the present invention, will be described with reference to FIG.
　図１に示された本発明の第１実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムは、燃料の微粉炭を空気と共に燃焼させて高温の燃焼ガスを生成し、この燃焼ガスを熱源として熱交換して高温の蒸気を生成して蒸気タービン等の蒸気供給先（図示せず）に供給する微粉炭焚きボイラ５０を備えている。 The mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to the first embodiment of the present invention shown in FIG. 1 combusts pulverized coal of fuel together with air to generate high-temperature combustion gas, and this combustion gas Is used as a heat source to generate a high-temperature steam and supply a steam supply destination (not shown) such as a steam turbine.
　燃料と空気とを燃焼させて燃焼排ガスを発生させる燃焼排ガスの発生源である微粉炭焚きボイラ５０から排出された燃焼排ガスを処理する燃焼排ガス処理システムは、微粉炭焚きボイラ５０の下流側にそれぞれ設置されており、該微粉炭焚きボイラ５０から流下する燃焼排ガス２１中の窒素酸化物（以下ＮＯｘと称する）を低減する脱硝装置５１と、脱硝装置５１の下流側に位置して燃焼排ガス２１中の燃焼灰を除去する集塵装置１と、集塵装置１の下流側に位置して燃焼排ガス２１中の硫黄酸化物（以下ＳＯｘと称する）を除去する脱硫装置２とから構成されている。 A combustion exhaust gas treatment system for treating combustion exhaust gas discharged from a pulverized coal burning boiler 50, which is a source of combustion exhaust gas that generates combustion exhaust gas by burning fuel and air, is disposed downstream of the pulverized coal burning boiler 50, respectively. A NOx removal device 51 for reducing nitrogen oxide (hereinafter referred to as NOx) in the flue gas 21 flowing down from the pulverized coal-fired boiler 50 and a downstream side of the NOx removal device 51 and in the flue gas 21 The dust collector 1 removes the combustion ash and the desulfurizer 2 that is located downstream of the dust collector 1 and removes sulfur oxide (hereinafter referred to as SOx) in the combustion exhaust gas 21.
　脱硫装置２の下流側には、燃焼排ガス２１中のＣＯ２を回収する二酸化炭素回収設備として、燃焼排ガス２１中の水分を除去する脱水装置３と、この脱水装置３の下流側に設置されて水分を除去した燃焼排ガス中のＣＯ２を圧縮する圧縮機４と、この圧縮機４で圧縮されたＣＯ２を冷却して液化する冷却器５’が備えられている。 On the downstream side of the desulfurization device 2, as a carbon dioxide recovery facility for recovering CO 2 in the combustion exhaust gas 21, a dehydration device 3 for removing moisture in the combustion exhaust gas 21 and a downstream side of the dehydration device 3 are installed. A compressor 4 that compresses CO 2 in the combustion exhaust gas from which moisture has been removed, and a cooler 5 ′ that cools and liquefies the CO 2 compressed by the compressor 4 are provided.
　この脱水装置３で燃焼排ガス２１中から除去された水分は水２２として脱水装置３から外部に排出される。 The water removed from the combustion exhaust gas 21 by the dehydrator 3 is discharged as water 22 from the dehydrator 3 to the outside.
　そして微粉炭焚きボイラ５０から排出された燃焼排ガス２１に含まれたＨｇ０は、脱水装置３と圧縮機４との間に設置された後述する金属水銀吸着塔１１及び１１’の内部に積層された金属水銀吸着剤によって燃焼排ガス２１中のＨｇ０を吸着させることによって燃焼排ガス２１から直接除去される。 Then, Hg 0 contained in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 is stacked inside metal mercury adsorption towers 11 and 11 ′ described later installed between the dehydrator 3 and the compressor 4. It is directly removed from the combustion exhaust gas 21 by adsorbing Hg 0 in the combustion exhaust gas 21 with the metal mercury adsorbent.
　前記金属水銀吸着塔１１及び１１’を流下することによって燃焼排ガス２１に含まれたＨｇ０が吸着除去された燃焼排ガス２１は、その下流側に設置された圧縮機４に流入して圧縮され、冷却器５’で冷却されて前記燃焼排ガス２１中のＣＯ２は液化することになるが、前記圧縮機４の圧縮と冷却器５’の冷却によってＨｇ０が吸着除去された燃焼排ガス２１中のＣＯ２は液化されたＣＯ２２３と、液化しない非凝縮性ガス２４になり、液化されたＣＯ２２３は前記冷却器５’から液化ＣＯ２の貯蔵設備（図示せず）に供給され、非凝縮性ガス２４は前記冷却器５’から更に下流側に流下して外部に排出されるように構成されている。 The combustion exhaust gas 21 from which Hg 0 contained in the combustion exhaust gas 21 is adsorbed and removed by flowing down the metal mercury adsorption towers 11 and 11 ′ flows into the compressor 4 installed on the downstream side thereof and is compressed, The CO 2 in the flue gas 21 is liquefied by being cooled by the cooler 5 ′, but the Hg 0 is adsorbed and removed by the compression of the compressor 4 and the cooling of the cooler 5 ′. The CO 2 becomes liquefied CO 2 23 and a non-condensable gas 24 that does not liquefy, and the liquefied CO 2 23 is supplied from the cooler 5 ′ to a storage facility (not shown) for liquefied CO 2. The condensable gas 24 is configured to flow further downstream from the cooler 5 ′ and be discharged to the outside.
　前記微粉炭焚きボイラ５０における微粉炭の燃焼は、ＣＯ２回収に適した酸素燃焼を行うが、微粉炭焚きボイラ５０から排出された燃焼排ガス２１の一部を集塵装置１の下流側から燃焼排ガス循環ライン２５を通じて微粉炭焚きボイラ５０に供給するようにして、燃焼排ガス２１の一部が微粉炭焚きボイラ５０に循環するように構成する。 The combustion of the pulverized coal in the pulverized coal burning boiler 50 performs oxygen combustion suitable for CO 2 recovery, but a part of the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 is burned from the downstream side of the dust collector 1. A part of the combustion exhaust gas 21 is configured to circulate to the pulverized coal burning boiler 50 so as to be supplied to the pulverized coal burning boiler 50 through the exhaust gas circulation line 25.
　微粉炭焚きボイラ５０で生成して排出される燃焼排ガス２１中の水銀の形態には、金属水銀Ｈｇ０と塩化水銀ＨｇＣｌ２がある。微粉炭焚きボイラ５０ではＨｇ０が主であり、微粉炭焚きボイラ５０の下流に設置された窒素酸化物を低減する脱硝装置５１の内部に載置された触媒によってＨｇ０がＨｇＣｌ２に変換される。 The forms of mercury in the combustion exhaust gas 21 produced and discharged by the pulverized coal burning boiler 50 include metallic mercury Hg 0 and mercury chloride HgCl 2 . In the pulverized coal burning boiler 50, Hg 0 is mainly used, and Hg 0 is converted into HgCl 2 by the catalyst placed inside the denitration device 51 that reduces nitrogen oxides installed downstream of the pulverized coal burning boiler 50. The
　脱硝装置５１の触媒でＨｇ０がＨｇＣｌ２に変換されることにより、変換されたこのＨｇＣｌ２は燃焼排ガス２１中に含まれた燃焼灰に吸着し、脱硝装置５１の下流側に設置された集塵装置１によって除去される。さらに、集塵装置１の下流側に設置された水を噴霧する脱硫装置２によって前記ＨｇＣｌ２は水に溶解させて除去することができる。 By converting Hg 0 into HgCl 2 by the catalyst of the denitration device 51, the converted HgCl 2 is adsorbed by the combustion ash contained in the combustion exhaust gas 21, and is collected on the downstream side of the denitration device 51. It is removed by the dust device 1. Further, the HgCl 2 can be dissolved in water and removed by a desulfurization device 2 that sprays water installed downstream of the dust collector 1.
　一方、燃焼排ガス２１中のＨｇ０は燃焼灰への吸着性、水への溶解性がないため、何も処理しない場合にはこのＨｇ０は燃焼排ガス２１と共に後流まで流下して煙突出口から大気に放出されることになる。 On the other hand, Hg 0 in the combustion exhaust gas 21 has no adsorptivity to combustion ash and no solubility in water, so when nothing is treated, this Hg 0 flows down to the downstream with the combustion exhaust gas 21 from the smoke outlet. Will be released to the atmosphere.
　微粉炭焚きボイラ５０では、ボイラ出口のＮＯｘ濃度は１００ｐｐｍから２００ｐｐｍの範囲であり、微粉炭焚きボイラ５０の下流側に設置した脱硝装置５１によって約３０ｐｐｍまで低減させた後に、燃焼排ガス処理システムの最下流に設置された煙突（図示せず）から大気に排出させている。 In the pulverized coal-fired boiler 50, the NOx concentration at the boiler outlet is in the range of 100 ppm to 200 ppm. After being reduced to about 30 ppm by the denitration device 51 installed on the downstream side of the pulverized coal-fired boiler 50, the most of the combustion exhaust gas treatment system. A chimney (not shown) installed downstream is discharged into the atmosphere.
　尚、ボイラ内脱硝技術の技術開発が進み、微粉炭焚きボイラ５０のボイラ出口でのＮＯｘ濃度が３０ｐｐｍに低減できれば微粉炭焚きボイラ５０の下流側に設置する脱硝装置５１が不要となるか、或いは脱硝装置５１によってＮＯｘ濃度を更に低減させて煙突から大気に排出させることが可能となる。 If the technical development of the denitration technology in the boiler advances and the NOx concentration at the boiler outlet of the pulverized coal burning boiler 50 can be reduced to 30 ppm, the denitration device 51 installed on the downstream side of the pulverized coal burning boiler 50 becomes unnecessary, or The NOx concentration can be further reduced by the denitration device 51 and discharged from the chimney to the atmosphere.
　また、微粉炭焚きボイラ５０における酸素燃焼？ではガス中の窒素分がなくなることからＮＯｘ濃度が低く、脱硝装置５１を設置することが不要になる可能性もある。 Also, oxygen combustion in pulverized coal fired boiler 50? Then, since there is no nitrogen content in the gas, the NOx concentration is low, and there is a possibility that it is not necessary to install the denitration device 51.
　仮に触媒によってＨｇ０をＨｇＣｌ２に変換する脱硝装置５１が微粉炭焚きボイラ５０の下流に設置されていない場合を想定すると、微粉炭焚きボイラ５０から排出された燃焼排ガス２１中のＨｇ０はＨｇＣｌ２に変換されずに下流側に排出されることになるので、Ｈｇ０をこの燃焼排ガス２１中から直接除去することが必要になる。 Assuming that a denitration device 51 that converts Hg 0 to HgCl 2 by a catalyst is not installed downstream of the pulverized coal burning boiler 50, Hg 0 in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50 is HgCl. since is discharged to the downstream side without being converted into 2, it is necessary to directly remove the Hg 0 from in the combustion exhaust gas 21.
　そこで、本実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいては、金属水銀ガス吸着塔１１及び１１’を脱水装置３と圧縮機４の間に並列に配設して、燃焼排ガス２１中から金属水銀Ｈｇ０を吸着して直接除去するようにした。 Therefore, in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas according to the present embodiment, the metal mercury gas adsorption towers 11 and 11 ′ are arranged in parallel between the dehydrator 3 and the compressor 4 to perform combustion. Metal mercury Hg 0 was adsorbed from the exhaust gas 21 and directly removed.
　前記金属水銀吸着塔１１及び１１’の内部には金属水銀吸着剤となるニッケル（以下Ｎｉと称する）を含む合金を板状吸着剤にして積層している。この金属水銀吸着剤に使用されるＮｉを含む合金としては、例えば、ＳＵＳが挙げられる。 In the metal mercury adsorption towers 11 and 11 ', an alloy containing nickel (hereinafter referred to as Ni) serving as a metal mercury adsorbent is laminated as a plate adsorbent. Examples of the alloy containing Ni used for the metal mercury adsorbent include SUS.
　ＳＵＳを構成する主元素はマンガン、ニッケル、クロムであり、いずれも遷移金属である。遷移金属はＨｇ０と結合してアマルガムを形成するため、Ｈｇ０を吸着する吸着剤として有効である。遷移金属であっても酸化されるとアマルガムを形成しなくなるため、望ましくは酸化されにくいニッケルが効果的な金属水銀吸着剤となる。 The main elements constituting SUS are manganese, nickel, and chromium, and all are transition metals. Since the transition metal combines with Hg 0 to form an amalgam, it is effective as an adsorbent for adsorbing Hg 0 . Even if a transition metal is oxidized, it does not form an amalgam. Therefore, nickel that is preferably not easily oxidized is an effective metal mercury adsorbent.
　図１を用いて、第１実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、水銀除去装置の構成を更に説明する。 Referring to FIG. 1, the configuration of the mercury removing device in the mercury removing system of the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment will be further described.
　並列に配設された流路には２基の金属水銀ガス吸着搭１１、１１’がそれぞれ設置されており、一方の金属水銀ガス吸着搭１１の上流側には入口バルブ１３が、下流側には出口バルブ１４がそれぞれ設けられ、同様に他方の金属水銀ガス吸着搭１１’の上流側には入口バルブ１３’が、下流側には出口バルブ１４’がそれぞれ設けている。 Two metal mercury gas adsorption towers 11 and 11 ′ are respectively installed in the flow paths arranged in parallel, and an inlet valve 13 is arranged on the upstream side of one metal mercury gas adsorption tower 11 on the downstream side. Each is provided with an outlet valve 14. Similarly, an inlet valve 13 ′ is provided on the upstream side of the other metal mercury gas adsorption tower 11 ′, and an outlet valve 14 ′ is provided on the downstream side.
　更に金属水銀ガス吸着搭１１、１１’への燃焼排ガス２１の通気の制御を行う制御装置１２が設置されており、この制御装置１２からの操作信号によって前記金属水銀ガス吸着搭１１、１１’の各入口バルブ１３、１３’、各出口バルブ１４、１４’の開閉を操作して、燃焼排ガス２１を金属水銀ガス吸着搭１１、１１’の何れか一方に切り替えて通気、又は双方に通気できるように制御している。 Further, a control device 12 for controlling the ventilation of the combustion exhaust gas 21 to the metal mercury gas adsorption towers 11 and 11 ′ is installed, and an operation signal from the control device 12 determines the metal mercury gas adsorption towers 11 and 11 ′. By opening / closing the inlet valves 13 and 13 ′ and the outlet valves 14 and 14 ′, the combustion exhaust gas 21 can be switched to one of the metal mercury gas adsorption towers 11 and 11 ′ so as to ventilate or both. Is controlling.
　前記金属水銀ガス吸着搭１１及び１１’の各出口バルブ１４及び１４’の後流側には水銀分析計１５、１５’が夫々設置されており、この金属水銀ガス吸着搭１１及び１１’を配設した並列の流路が合流した下流側の合流流路にも更に水銀分析計１５ｂが設置されて、合流流路を流下する燃焼排ガス２１中の水銀濃度の値を検出するようになっている。 Mercury analyzers 15 and 15 'are installed on the downstream side of the outlet valves 14 and 14' of the metal mercury gas adsorption towers 11 and 11 ', respectively, and the metal mercury gas adsorption towers 11 and 11' are arranged. A mercury analyzer 15b is also installed in the downstream merged flow channel where the parallel flow channels that have been merged join to detect the value of the mercury concentration in the combustion exhaust gas 21 flowing down the merged flow channel. .
　そして前記各水銀分析計１５、１５’、１５ｂによって計測された燃焼排ガス２１の水銀濃度の検出値はそれぞれ前記制御装置１２に入力され、この制御装置１２にて各水銀濃度の検出値と該制御装置１２で予め設定した水銀濃度の上限値との比較に基づいて操作信号を出力して前記金属水銀ガス吸着搭１１、１１’の各入口バルブ１３、１３’、各出口バルブ１４、１４’の開閉を操作し、燃焼排ガス２１が金属水銀ガス吸着搭１１、１１’の何れか一方に通気、又は双方に通気するように制御する。 The detected mercury concentration values of the flue gas 21 measured by the mercury analyzers 15, 15 ′ and 15 b are input to the control device 12, respectively. An operation signal is output based on the comparison with the upper limit value of the mercury concentration set in advance by the apparatus 12, and the inlet valves 13, 13 'and outlet valves 14, 14' of the metal mercury gas adsorption towers 11, 11 'are output. The opening / closing operation is performed, and the combustion exhaust gas 21 is controlled to be ventilated to one or both of the metal mercury gas adsorption towers 11 and 11 ′.
　例えば、一方の金属水銀ガス吸着搭１１に燃焼排ガス２１を通気して単独で運転させ、他方の金属水銀ガス吸着搭１１’には燃焼排ガス２１を通気しないで待機させるように制御することも可能である。 For example, it is possible to control so that the combustion exhaust gas 21 is vented to one metal mercury gas adsorption tower 11 and operated alone, and the other metal mercury gas adsorption tower 11 ′ is made to stand by without venting the combustion exhaust gas 21. It is.
　そして前記制御装置１２では各水銀分析計１５、１５’、１５ｂで計測した燃焼排ガス２１の水銀濃度の検出値を連続して監視し、例えば前記一方の金属水銀ガス吸着搭１１の下流側に設置した水銀分析計１５によって該一方の金属水銀ガス吸着搭１１を流下した燃焼排ガス２１の水銀濃度の検出値が該一方の金属水銀ガス吸着搭１１の内部に積層されたＨｇ０を吸着する金属水銀吸着剤の吸着性能の低下によって予め設定した水銀濃度の上限値にまで達したことを検出した場合には、制御装置１２からの操作信号によって一方の金属水銀ガス吸着搭１１の入口バルブ１３及び出口バルブ１４を閉操作して前記一方の金属水銀ガス吸着搭１１の運転を停止すると共に、他方の金属水銀ガス吸着塔１１’の入口バルブ１３’及び出口バルブ１４’を開操作して燃焼排ガス２１をこの他方の金属水銀ガス吸着塔１１’に通気して前記他方の金属水銀ガス吸着塔１１’の運転に切り替える。 The control device 12 continuously monitors the detected value of the mercury concentration of the combustion exhaust gas 21 measured by the mercury analyzers 15, 15 ′, 15 b and is installed, for example, on the downstream side of the one metal mercury gas adsorption tower 11. The detected mercury concentration of the flue gas 21 flowing down the one metal mercury gas adsorption tower 11 by the mercury analyzer 15 is a metal mercury that adsorbs Hg 0 stacked inside the one metal mercury gas adsorption tower 11. When it is detected that the upper limit value of the mercury concentration set in advance has been reached due to a decrease in the adsorption performance of the adsorbent, the inlet valve 13 and the outlet of one of the metallic mercury gas adsorption towers 11 are detected by an operation signal from the controller 12 The valve 14 is closed to stop the operation of the one metal mercury gas adsorption tower 11, and the inlet valve 13 ′ and the outlet valve 14 ′ of the other metal mercury gas adsorption tower 11 ′ are turned on. Operation and 'vented to the other metal mercury gas adsorption tower 11' a flue gas 21 this other metal mercury gas adsorption tower 11 is switched to the operation of the.
　前記他方の金属水銀ガス吸着塔１１’の運転に切り替えた後は、この他方の金属水銀ガス吸着塔１１’の下流側に設置した水銀分析計１５’によって前記他方の金属水銀ガス吸着塔１１’を流下した燃焼排ガス２１中の水銀濃度の値を検出して監視を行う。 After switching to the operation of the other metal mercury gas adsorption tower 11 ′, the other metal mercury gas adsorption tower 11 ′ is performed by a mercury analyzer 15 ′ installed on the downstream side of the other metal mercury gas adsorption tower 11 ′. The mercury concentration value in the flue gas 21 flowing down is detected and monitored.
　ここで、前記制御装置１２に設定されている燃焼排ガス２１中の水銀濃度の上限値は、前記金属水銀ガス吸着搭１１、１１’の下流側に設置した圧縮機４に用いられている金属部材が許容できる燃焼排ガス２１中の水銀濃度に基づいて設定される。 Here, the upper limit value of the mercury concentration in the combustion exhaust gas 21 set in the control device 12 is a metal member used in the compressor 4 installed on the downstream side of the metal mercury gas adsorption towers 11, 11 ′. Is set based on the mercury concentration in the combustion exhaust gas 21 that can be tolerated.
　前記したように燃焼排ガス２１を一方の金属水銀ガス吸着塔１１への通気から他方の金属水銀ガス吸着塔１１’への通気に変更して前記他方の金属水銀ガス吸着塔１１’の単独運転に切り替え、前記一方の金属水銀ガス吸着塔１１が運転を停止させている間にこの一方の金属水銀ガス吸着搭１１では、吸着塔の内部に積層されている吸着性能の低下した金属水銀吸着剤を新しい金属水銀吸着剤に入れ替えて待機状態にする。 As described above, the combustion exhaust gas 21 is changed from ventilation to one metal mercury gas adsorption tower 11 to ventilation to the other metal mercury gas adsorption tower 11 ′, so that the other metal mercury gas adsorption tower 11 ′ is operated independently. While the one metal mercury gas adsorption tower 11 is switched off, the one metal mercury gas adsorption tower 11 removes the metal mercury adsorbent with reduced adsorption performance stacked inside the adsorption tower. Replace with a new metal mercury adsorbent and put it on standby.
　その後、前記他方の金属水銀ガス吸着搭１１’を単独で運転させ、この他方の金属水銀ガス吸着搭１１’の下流側に設置した水銀分析計１５’によって該他方の金属水銀ガス吸着搭１１’を流下した燃焼排ガス２１の水銀濃度の検出値がこの他方の金属水銀ガス吸着搭１１’の内部に積層されたＨｇ０を吸着する金属水銀吸着剤の吸着性能も低下によって予め設定した水銀濃度の上限値にまで達したことを検出した場合には、前記制御装置１２からの操作信号によって待機状態にあった一方の金属水銀ガス吸着搭１１の入口バルブ１３及び出口バルブ１４を開操作し、前記他方の金属水銀ガス吸着搭１１’及び前記一方の金属水銀ガス吸着搭１１の両方に燃焼排ガス２１を一時的に通気させるようにして、前記他方の金属水銀ガス吸着搭１１’及び一方の金属水銀ガス吸着搭１１の双方を運転させる。 Thereafter, the other metal mercury gas adsorption tower 11 ′ is operated alone, and the other metal mercury gas adsorption tower 11 ′ is installed by a mercury analyzer 15 ′ installed downstream of the other metal mercury gas adsorption tower 11 ′. The detection value of the mercury concentration of the combustion exhaust gas 21 flowing down the gas has a predetermined mercury concentration by reducing the adsorption performance of the metal mercury adsorbent that adsorbs Hg 0 stacked inside the other metal mercury gas adsorption tower 11 ′. When it is detected that the upper limit value has been reached, the inlet valve 13 and the outlet valve 14 of one of the metal mercury gas adsorption towers 11 in the standby state are opened by the operation signal from the control device 12, Combustion exhaust gas 21 is temporarily vented to both the other metal mercury gas adsorption tower 11 ′ and the one metal mercury gas adsorption tower 11 so that the other metal mercury gas adsorption tower 11 ′ and one metal mercury gas adsorption tower 11 ′ It is operated both metal mercury gas adsorption tower 11.
　この金属水銀ガス吸着搭１１及び１１’の双方を一時的に運転させる場合には、前記並列の流路が合流した下流側の合流流路に設置された水銀分析計１５ｂによって前記金属水銀ガス吸着搭１１及び１１’の双方からこの合流流路を流下する燃焼排ガス２１中の水銀濃度の値を検出して監視し、前記金属水銀ガス吸着搭１１及び１１’の双方によって燃焼排ガス２１中の水銀濃度を低減させて、一方の金属水銀ガス吸着搭１１と他方の金属水銀ガス吸着搭１１’との運転の切り替えに伴なう燃焼排ガス２１中の水銀濃度の増加を抑制させている。 When both the metal mercury gas adsorption towers 11 and 11 'are temporarily operated, the metal mercury gas adsorption is performed by the mercury analyzer 15b installed in the downstream merge channel where the parallel channels merge. Mercury concentration value in the flue gas 21 flowing down this merged flow path from both the towers 11 and 11 ′ is detected and monitored, and the mercury in the flue gas 21 is detected by both the metal mercury gas adsorption towers 11 and 11 ′. The concentration is reduced to suppress an increase in the mercury concentration in the combustion exhaust gas 21 due to the operation switching between the one metal mercury gas adsorption tower 11 and the other metal mercury gas adsorption tower 11 ′.
　ところで、一時的に燃焼排ガス２１を通気中の一方の前記金属水銀ガス吸着搭１１又は１１’を流下する燃焼排ガス２１中の水銀濃度の値が突発的に急上昇した場合は、前記金属水銀ガス吸着搭１１、は１１’の下流側の合流流路に設置した水銀分析計１５ｂでこの合流流路を流下する燃焼排ガス２１中の水銀濃度の急上昇を捉えて、前記金属水銀ガス吸着搭１１への燃焼排ガス２１の通気だけでなく、待機中の他方の前記金属水銀ガス吸着搭１１’にも燃焼排ガス２１を通気させて前記金属水銀ガス吸着搭１１及び１１’の双方を運転する並列運転にして、燃焼排ガス２１中の水銀濃度が急上昇した水銀を低減させる運転を行う。 By the way, when the value of the mercury concentration in the combustion exhaust gas 21 flowing down one of the metal mercury gas adsorption towers 11 or 11 ′ temporarily ventilating the combustion exhaust gas 21 suddenly rises suddenly, the metal mercury gas adsorption is performed. The tower 11 is a mercury analyzer 15b installed in the confluence channel on the downstream side of 11 ′, and captures a sudden rise in the mercury concentration in the combustion exhaust gas 21 flowing down the confluence channel, and is applied to the metal mercury gas adsorption tower 11. In addition to the ventilation of the combustion exhaust gas 21, the parallel operation in which both the metal mercury gas adsorption towers 11 and 11 ′ are operated by aeration of the combustion exhaust gas 21 to the other metal mercury gas adsorption tower 11 ′ on standby. Then, an operation for reducing mercury in which the mercury concentration in the combustion exhaust gas 21 has rapidly increased is performed.
　本実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおける燃焼排ガス２１中のＣＯ２の回収は、圧縮機４で加圧したＣＯ２を冷却器５’で冷却して液化させたＣＯ２２３にして、前記冷却器５’からこの液化させたＣＯ２２３の回収を行うようにし、液化しない燃焼排ガス２１の非凝縮性ガス２４は前記冷却器５’で液化したＣＯ２２３と分離させて下流側に流下させる。 The recovery of CO 2 in the combustion exhaust gas 21 in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment is performed by cooling the CO 2 pressurized by the compressor 4 with the cooler 5 ′ and liquefying it. and 2 23, the 'from to perform the recovery of CO 2 23, which is liquefied, non-condensable gas 24 of the combustion exhaust gas 21 which is not liquefied is the cooler 5' cooler 5 separated from the CO 2 23 liquefied by And let it flow down downstream.
　燃焼排ガス２１中のＣＯ２の回収率を更に高くするためには、後述する図７の実施例に示したように圧縮機を複数個設置して、前段の圧縮機による圧縮で温度上昇させた燃焼排ガス２１を、後段の圧縮機で更に圧縮する多段圧縮を行い、この多段圧縮された燃焼排ガス２１中のＣＯ２を冷却器で冷却して液化させることが必要になる。 In order to further increase the CO 2 recovery rate in the combustion exhaust gas 21, a plurality of compressors were installed as shown in an example of FIG. 7 to be described later, and the temperature was increased by compression by the compressor in the previous stage. It is necessary to perform multistage compression in which the combustion exhaust gas 21 is further compressed by a subsequent compressor, and CO 2 in the combustion exhaust gas 21 compressed in the multistage is cooled by a cooler to be liquefied.
　図２は図１に示した第１実施例の燃焼排ガス中の二酸化炭素回収設備における水銀除去システムを構成する金属水銀ガス吸着塔１１、１１’の内部に設置される金属水銀吸着剤である板状吸着剤３１の一具体例を示している。 2 is a plate that is a metal mercury adsorbent installed in the metal mercury gas adsorption towers 11 and 11 ′ constituting the mercury removal system in the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment shown in FIG. A specific example of the adsorbent 31 is shown.
　図２において、燃焼排ガス２１中のＨｇ０を吸着する金属水銀吸着剤を構成する板状吸着剤３１は、金属水銀ガス吸着塔１１、１１’の内部に流入する燃焼排ガス２１の流れ方向に沿って幅方向に離間させて配置され、隣接した板状吸着剤３１との間に燃焼排ガス２１が流下する流路２１ａを形成するように複数枚積層した構造となっている。 In FIG. 2, the plate-like adsorbent 31 constituting the metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 is along the flow direction of the combustion exhaust gas 21 flowing into the metal mercury gas adsorption towers 11, 11 ′. In this structure, a plurality of layers are stacked so as to form a flow path 21a through which the flue gas 21 flows down between adjacent plate-like adsorbents 31.
　また、金属水銀吸着剤を粒子として、金属水銀ガス吸着塔１１、１１’内にこの粒子を充填してもよいが、燃焼排ガス２１の通気性が悪くなるため、通気性のよい板状吸着剤３１の積層構造を採用した。 Further, the metal mercury adsorbent may be used as particles, and the particles may be filled in the metal mercury gas adsorption towers 11 and 11 '. A 31-layer structure was adopted.
　前記板状吸着剤３１の交換は、金属水銀吸着塔１１、１１’の上面、あるいは燃焼排ガス２１の流出入口がある側面を取り外し、吸着性能が低下した板状吸着剤３１を１枚ずつ新しい板状吸着剤３１と交換するか、あるいは、板状吸着剤３１を積層できる型枠に設置して型枠ごと新しい板状吸着剤３１と交換すればよい。 The plate-shaped adsorbent 31 is replaced by removing the upper surfaces of the metal mercury adsorption towers 11 and 11 ′ or the side surface where the combustion exhaust gas 21 flows out, and replacing the plate-shaped adsorbent 31 with reduced adsorption performance one by one. The plate-like adsorbent 31 may be exchanged, or the plate-like adsorbent 31 may be installed in a mold that can be stacked and replaced with a new plate-like adsorbent 31 together with the mold.
　図３は図１に示した第１実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムを構成する金属水銀ガス吸着塔１１、１１’の内部に設置される金属水銀吸着剤である板状吸着剤３１の他の具体例を示す。 FIG. 3 is a plate that is a metal mercury adsorbent installed inside the metal mercury gas adsorption towers 11 and 11 ′ constituting the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment shown in FIG. Another specific example of the adsorbent 31 is shown.
　図３において、燃焼排ガス２１中のＨｇ０を吸着する金属水銀吸着剤を構成するハニカム状吸着剤３２は、燃焼排ガス２１を流下させる多数の空孔２１ｂが燃焼排ガスの流れの方向に沿うように形成された構造となっている。 In FIG. 3, the honeycomb adsorbent 32 constituting the metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 has a large number of holes 21b for flowing the combustion exhaust gas 21 along the flow direction of the combustion exhaust gas. It has a formed structure.
　金属水銀吸着剤を多数の空孔２１ｂを形成したハニカム状吸着剤３２の構成にすることによって、金属水銀吸着塔１１、１１’を流下する燃焼排ガス２１の圧力損失を小さくできる。また、ハニカムカム構造は、板状吸着剤の積層構造よりもＨｇ０を吸着する吸着面積を広くすることができる。 By making the metallic mercury adsorbent into the honeycomb adsorbent 32 having a large number of holes 21b, the pressure loss of the combustion exhaust gas 21 flowing down the metallic mercury adsorption towers 11 and 11 ′ can be reduced. Further, the honeycomb cam structure can make the adsorption area for adsorbing Hg 0 wider than the laminated structure of the plate-like adsorbent.
　また、金属水銀吸着剤に使用されるニッケルと金属水銀との反応、すなわちアマルガムを生成する反応は、高温ほど反応速度は高いが、高温過ぎるとアマルガムが分解し、金属水銀を放出する。 Also, the reaction between nickel and metal mercury used in the metal mercury adsorbent, that is, the reaction that generates amalgam has a higher reaction rate as the temperature is higher. However, if the temperature is too high, the amalgam decomposes and releases metal mercury.
　燃焼排ガス２１中のＨｇ０を吸着する金属水銀吸着剤には金属水銀を吸着するのに適した温度範囲が存在する。金属水銀吸着剤に使用されるＮｉを含む合金としてＳＵＳへの水銀吸着性能を評価した試験では、ＳＵＳ管の温度が１７０℃から３７０℃の範囲で良好な結果が得られており、よって金属水銀吸着剤は１７０℃から３７０℃の温度範囲で使用されることが望ましい。 The metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 has a temperature range suitable for adsorbing metal mercury. In the test for evaluating the mercury adsorption performance to SUS as an alloy containing Ni used for the metal mercury adsorbent, good results were obtained when the temperature of the SUS tube ranged from 170 ° C to 370 ° C. The adsorbent is desirably used in a temperature range of 170 ° C to 370 ° C.
　尚、燃焼排ガス２１の温度が、この温度範囲よりも低い場合には、金属水銀吸着剤を上記の温度範囲にまで加熱する手段を備えることが望ましい。 In addition, when the temperature of the combustion exhaust gas 21 is lower than this temperature range, it is desirable to provide means for heating the metal mercury adsorbent to the above temperature range.
　図４は図１に示した第１実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムを構成する金属水銀ガス吸着塔１１、１１’の内部に設置される金属水銀吸着剤である板状吸着剤３１に加熱手段を備えた更に他の具体例を示す。 4 is a plate which is a metal mercury adsorbent installed inside the metal mercury gas adsorption towers 11 and 11 ′ constituting the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the first embodiment shown in FIG. Another specific example in which the adsorbent 31 is provided with heating means will be described.
　図４において、燃焼排ガス２１中のＨｇ０を吸着する金属水銀吸着剤を構成する板状吸着剤３１は、ヒータ３３をこの板状吸着剤３１で挟み込む構造となっている。ヒータ３３はニクロム線のようなニッケルを含む材料が望ましい。 In FIG. 4, a plate-like adsorbent 31 constituting a metal mercury adsorbent that adsorbs Hg 0 in the combustion exhaust gas 21 has a structure in which a heater 33 is sandwiched between the plate-like adsorbents 31. The heater 33 is preferably made of a material containing nickel such as nichrome wire.
　板状吸着剤３１のヒータ３３が燃焼排ガス２１に接触しても、ヒータ３３による加熱温度がアマルガムの分解温度以上になるとＨｇ０は板状吸着剤３１に吸着しなくなる。 Even if the heater 33 of the plate-like adsorbent 31 comes into contact with the combustion exhaust gas 21, if the heating temperature by the heater 33 becomes equal to or higher than the decomposition temperature of the amalgam, Hg 0 will not be adsorbed on the plate-like adsorbent 31.
　また、ヒータ３３の表面にアマルガムを生成したとしても、ヒータ３３をアマルガムの分解温度以上に加熱すれば、Ｈｇ０を放出して再生することができる。 Further, even produced an amalgam on the surface of the heater 33, by heating the heater 33 to a temperature higher than the decomposition temperature of the amalgam can be regenerated by releasing Hg 0.
　したがって、ヒータ３３を設置する板状吸着剤３１に形成された空間は密閉の必要はなく、製作が簡単になる。 Therefore, the space formed in the plate-like adsorbent 31 in which the heater 33 is installed does not need to be sealed, and the manufacture is simplified.
　長時間の使用によって燃焼排ガス２１中のＨｇ０の吸着性能が低下した金属水銀吸着剤である板状吸着剤３１は、本実施例の燃焼排ガス中の水銀除去システムとは別の場所にて加熱再生処理することによって金属水銀吸着剤として再使用することが可能である。 Plate adsorbent 31 adsorb performance is metallic mercury adsorbent reduction of Hg 0 in the combustion exhaust gas 21 used for a long time, the heating in a separate location from the mercury removal system of the combustion exhaust gas of the present embodiment It can be reused as a metal mercury adsorbent by reprocessing.
　次に本発明の第２実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムについて図５を用いて説明する。 Next, a mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to a second embodiment of the present invention will be described with reference to FIG.
　図５に示した第２実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムは、図１に示した先の実施例の燃焼排ガス中の水銀除去システムと基本的な構成は同じであるので、両者に共通した構成の説明は省略し、相違した構成についてのみ以下に説明する。 The mercury removal system for carbon dioxide recovery equipment in the combustion exhaust gas of the second embodiment shown in FIG. 5 has the same basic configuration as the mercury removal system in the combustion exhaust gas of the previous embodiment shown in FIG. Therefore, the description of the configuration common to both is omitted, and only the different configuration will be described below.
　本実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいては、図５に示したのように、微粉炭焚きボイラ５０から排出された燃焼排ガス２１中のＳＯｘを除去する脱硫装置２と、燃焼排ガス２１中の水分を除去する脱水装置３との間に、燃焼排ガス２１中のＨｇ０を吸着して除去する金属水銀吸着剤を内部に積層した金属水銀吸着塔１１、１１’が並列に配設されており、これらの金属水銀吸着塔１１、１１’の後流となる前記脱水装置３の下流側に燃焼排ガス２１中のＣＯ２を圧縮する圧縮機４と、この圧縮機４で圧縮されたＣＯ２を冷却して液化し、液化したＣＯ２２３を回収する冷却器５’が設置された構成となっている。 In the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment, as shown in FIG. 5, the desulfurization device 2 for removing SOx in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50, Between the dehydrator 3 for removing moisture in the combustion exhaust gas 21, metal mercury adsorption towers 11, 11 ′ in which a metal mercury adsorbent that adsorbs and removes Hg 0 in the combustion exhaust gas 21 is laminated are arranged in parallel. The compressor 4 compresses CO 2 in the combustion exhaust gas 21 on the downstream side of the dehydrator 3 that is the downstream of these metal mercury adsorption towers 11, 11 ′. the compressed CO 2 is liquefied by cooling, the cooler 5 'is in the installed configuration for recovering CO 2 23 liquefied.
　本実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおける燃焼排ガス２１中のＣＯ２の回収は、圧縮機４で加圧したＣＯ２を冷却器５’で冷却して液化したＣＯ２としてこの冷却器５’から回収を行い、液化しない燃焼排ガス２１の非凝縮性ガス２４は前記冷却器５’で液化したＣＯ２２３と分離させて下流側に流下させる。 Recovery of CO 2 in the combustion exhaust gas 21 in the mercury removal system of the carbon dioxide recovery equipment in combustion exhaust gas of the present embodiment, the compressor 4 pressurized CO 2 is liquefied by cooling by the cooler 5 'in the CO 2 The non-condensable gas 24 of the combustion exhaust gas 21 that is not liquefied is separated from the CO 2 23 that has been liquefied by the cooler 5 ′ and is caused to flow downstream.
　燃焼排ガス２１中のＣＯ２の回収率を更に高くするためには、後述する図７の実施例に示したように圧縮機を複数個設置して、前段の圧縮機による圧縮で温度上昇させた燃焼排ガス２１を、後段の圧縮機で更に圧縮する多段圧縮を行い、この多段圧縮された燃焼排ガス２１中のＣＯ２を冷却器で冷却して液化させることが必要になる。 In order to further increase the CO 2 recovery rate in the combustion exhaust gas 21, a plurality of compressors were installed as shown in an example of FIG. 7 to be described later, and the temperature was increased by compression by the compressor in the previous stage. It is necessary to perform multistage compression in which the combustion exhaust gas 21 is further compressed by a subsequent compressor, and CO 2 in the combustion exhaust gas 21 compressed in the multistage is cooled by a cooler to be liquefied.
　本実施例によれば、前記金属水銀吸着塔１１、１１’を脱水装置３の上流側の温度の高い領域に並列に配設させた構成なので、この金属水銀吸着塔１１、１１’に流入する燃焼排ガス２１の温度が高くなり、燃焼排ガス２１中のＨｇ０を金属水銀吸着塔１１、１１’の金属水銀吸着剤に吸着させてアマルガムを形成し易くできる。 According to the present embodiment, the metal mercury adsorption towers 11 and 11 ′ are arranged in parallel in the high temperature region on the upstream side of the dehydration apparatus 3, and therefore flow into the metal mercury adsorption towers 11 and 11 ′. The temperature of the combustion exhaust gas 21 becomes high, and Hg 0 in the combustion exhaust gas 21 can be adsorbed on the metal mercury adsorbent of the metal mercury adsorption towers 11 and 11 ′ to easily form an amalgam.
　次に本発明の第３実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムについて図６を用いて説明する。 Next, a mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to a third embodiment of the present invention will be described with reference to FIG.
　図６に示した第３実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムは、図１に示した先の実施例の燃焼排ガス中の水銀除去システムと基本的な構成は同じであるので、両者に共通した構成の説明は省略し、相違した構成についてのみ以下に説明する。 The mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the third embodiment shown in FIG. 6 has the same basic configuration as the mercury removal system in the combustion exhaust gas of the previous embodiment shown in FIG. Therefore, the description of the configuration common to both is omitted, and only the different configuration will be described below.
　本実施例の燃焼排ガス中の二酸化炭素回収設備における水銀除去システムにおいては、図６に示したのように、微粉炭焚きボイラ５０から排出された燃焼排ガス２１中の燃焼灰を除去する集塵装置１と、燃焼排ガス２１中のＳＯｘを除去する脱硫装置２との間に、燃焼排ガス２１中のＨｇ０を吸着して除去する金属水銀吸着剤を内部に積層した金属水銀吸着塔１１、１１’が並列に配設されており、これらの金属水銀吸着塔１１、１１’の後流の前記脱硫装置２の下流側に燃焼排ガス２１中の水分を除去する脱水装置３と、燃焼排ガス中のＣＯ２を圧縮して液化する圧縮機４と、この圧縮機４で圧縮されたＣＯ２を冷却して液化し、液化したＣＯ２２３を回収する冷却器５’が設置された構成となっている。 In the mercury removal system in the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment, as shown in FIG. 6, the dust collector for removing the combustion ash in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50. 1 and a desulfurizer 2 that removes SOx in the combustion exhaust gas 21, a metal mercury adsorption tower 11, 11 ′ in which a metal mercury adsorbent that adsorbs and removes Hg 0 in the combustion exhaust gas 21 is laminated. Are disposed in parallel, a dehydrator 3 for removing moisture in the combustion exhaust gas 21 downstream of the desulfurization device 2 downstream of the metal mercury adsorption towers 11 and 11 ′, and a CO in the combustion exhaust gas. a compressor 4 to liquefy by compressing 2, has become the compressor CO 2 compressed in the 4 and liquefied by cooling, liquefied CO 2 23 is cooler 5 'to recover the installed configuration .
　本実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムでは、燃焼排ガス２１中のＣＯ２の回収は、圧縮機４で加圧したＣＯ２を冷却器５’で冷却して液化したＣＯ２としてこの冷却器５’から回収を行い、液化しない燃焼排ガス２１の非凝縮性ガス２４は前記冷却器５’で液化したＣＯ２２３と分離させて下流側に流下させる。 In the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment, the CO 2 recovery in the combustion exhaust gas 21 is performed by liquefying CO 2 pressurized by the compressor 4 by cooling it with the cooler 5 ′. 2 , the non-condensable gas 24 of the combustion exhaust gas 21 that is not liquefied is separated from the CO 2 23 liquefied by the cooler 5 ′ and is caused to flow downstream.
　燃焼排ガス２１中のＣＯ２の回収率を更に高くするためには、後述する図７の実施例に示したように圧縮機を複数個設置して、前段の圧縮機による圧縮で温度上昇させた燃焼排ガス２１を、後段の圧縮機で更に圧縮する多段圧縮を行い、この多段圧縮された燃焼排ガス２１中のＣＯ２を冷却器で冷却して液化させることが必要になる。 In order to further increase the CO 2 recovery rate in the combustion exhaust gas 21, a plurality of compressors were installed as shown in an example of FIG. 7 to be described later, and the temperature was increased by compression by the compressor in the previous stage. It is necessary to perform multistage compression in which the combustion exhaust gas 21 is further compressed by a subsequent compressor, and CO 2 in the combustion exhaust gas 21 compressed in the multistage is cooled by a cooler to be liquefied.
　本実施例によれば、前記金属水銀吸着塔１１、１１’を脱硫装置２の上流側の温度が更に高い領域に並列に配設させた構成なので、この金属水銀吸着塔１１、１１’に流入する燃焼排ガス２１の温度が更に高くなり、燃焼排ガス２１中のＨｇ０を金属水銀吸着塔１１、１１’の金属水銀吸着剤に吸着させてアマルガムを更に形成し易くできる。 According to the present embodiment, the metal mercury adsorption towers 11 and 11 ′ are arranged in parallel in a region where the temperature on the upstream side of the desulfurization apparatus 2 is higher, and therefore flow into the metal mercury adsorption towers 11 and 11 ′. The temperature of the combustion exhaust gas 21 to be further increased, and Hg 0 in the combustion exhaust gas 21 can be adsorbed to the metal mercury adsorbent of the metal mercury adsorption towers 11 and 11 ′ to further easily form the amalgam.
　次に本発明の第４実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムについて図７を用いて説明する。 Next, a mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to a fourth embodiment of the present invention will be described with reference to FIG.
　図７に示した第４実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムは、図１に示した先の実施例の燃焼排ガス中の水銀除去システムと基本的な構成は同じであるので、両者に共通した構成の説明は省略し、相違した構成についてのみ以下に説明する。 The mercury removal system for carbon dioxide recovery equipment in the combustion exhaust gas of the fourth embodiment shown in FIG. 7 has the same basic configuration as the mercury removal system in the combustion exhaust gas of the previous embodiment shown in FIG. Therefore, the description of the configuration common to both is omitted, and only the different configuration will be described below.
　本実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいては、図７に示したのように、微粉炭焚きボイラ５０から排出された燃焼排ガス２１中の水分を除去する脱水装置３と、燃焼排ガス２１中のＨｇ０を吸着して除去する金属水銀吸着剤を内部に積層した並列に配設された金属水銀吸着塔１１、１１’との間に、燃焼排ガス２１中のＣＯ２を圧縮する圧縮機４が設置されている。 In the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment, as shown in FIG. 7, the dehydrator 3 for removing the moisture in the combustion exhaust gas 21 discharged from the pulverized coal burning boiler 50, CO 2 in the combustion exhaust gas 21 is placed between the metal mercury adsorption towers 11 and 11 ′ arranged in parallel with a metal mercury adsorbent that adsorbs and removes Hg 0 in the combustion exhaust gas 21. A compressor 4 for compression is installed.
　更に、並列に配設された金属水銀吸着塔１１、１１’の下流側には前記金属水銀吸着塔１１及び１１’を流下した燃焼排ガス２１を冷却する冷却器５が設けてあり、前記冷却器５の下流側には燃焼排ガス２１中のＣＯ２を圧縮する第２の圧縮機４’と、この第２の圧縮機４’で圧縮されたＣＯ２を冷却して液化し、液化したＣＯ２２３を回収する冷却器５’が設置された構成となっている。 Further, a cooler 5 for cooling the combustion exhaust gas 21 flowing down the metal mercury adsorption towers 11 and 11 ′ is provided on the downstream side of the metal mercury adsorption towers 11 and 11 ′ arranged in parallel. 5 'and, the second compressor 4' second compressor 4 on the downstream side of compressing CO 2 in the combustion exhaust gas 21 of liquefying CO 2 compressed in cooled, liquefied CO 2 The cooler 5 ′ for recovering 23 is installed.
　本実施例では圧縮機を前段の圧縮機４と後段の圧縮機４’との二段に設けた燃焼排ガス中の二酸化炭素回収設備における水銀除去システムを構成している。 In this embodiment, a mercury removal system is configured in a carbon dioxide recovery facility in combustion exhaust gas in which a compressor is provided in two stages of a front stage compressor 4 and a rear stage compressor 4 '.
　また本実施例においては、燃焼排ガス２１中のＨｇ０を吸着して除去する並列に配設された金属水銀吸着塔１１及び１１’は、冷却器５と後段の第２の圧縮機４’との間に配設した構成にしても良い。 Further, in this embodiment, the metal mercury adsorption towers 11 and 11 ′ arranged in parallel for adsorbing and removing Hg 0 in the combustion exhaust gas 21 include the cooler 5 and the second compressor 4 ′ at the subsequent stage. You may make it the structure arrange | positioned between.
　前記金属水銀吸着塔１１及び１１’の最適な設置位置は、燃焼排ガス２１の温度から決めることができる。金属水銀吸着塔１１及び１１’の内部に積層されるＨｇ０を吸着して除去する金属水銀吸着剤は、燃焼排ガス２１の温度が高温なほどＨｇ０の吸着性能が良くなるが、燃焼排ガス２１の温度がアマルガムの分解温度以上にまで高温になると逆に吸着性能が低下するためである。 The optimum installation position of the metal mercury adsorption towers 11 and 11 ′ can be determined from the temperature of the combustion exhaust gas 21. The metal mercury adsorbent that adsorbs and removes Hg 0 stacked inside the metal mercury adsorption towers 11 and 11 ′ improves the adsorption performance of Hg 0 as the temperature of the combustion exhaust gas 21 increases. This is because the adsorption performance is lowered when the temperature becomes higher than the decomposition temperature of the amalgam.
　前記冷却器５と後段の第２の圧縮機４’との間を流下する燃焼排ガス２１の温度は、前段の圧縮機４と冷却器５との間を流下する燃焼排ガス２１の温度よりも低くなるので、前段の圧縮機４と冷却器５の間を流下する前記燃焼排ガス２１の温度がアマルガムの分解温度以上の高温になるのであれば、冷却器５と後段の第２の圧縮機４’との間に上記したように並列に配設された金属水銀吸着塔１１及び１１’を設ければ良い。 The temperature of the combustion exhaust gas 21 flowing down between the cooler 5 and the second compressor 4 ′ in the subsequent stage is lower than the temperature of the combustion exhaust gas 21 flowing down between the compressor 4 in the previous stage and the cooler 5. Therefore, if the temperature of the combustion exhaust gas 21 flowing between the front compressor 4 and the cooler 5 is higher than the decomposition temperature of the amalgam, the cooler 5 and the second compressor 4 ′ of the rear stage. As described above, the metal mercury adsorption towers 11 and 11 'arranged in parallel may be provided between the two.
　本実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおける燃焼排ガス２１中のＣＯ２の回収は、後段の第２の圧縮機４’で加圧したＣＯ２を冷却器５’で冷却して液化したＣＯ２としてこの冷却器５’から回収を行い、液化しない燃焼排ガス２１の非凝縮性ガス２４は前記冷却器５’で液化したＣＯ２２３と分離させて下流側に流下させる。 The CO 2 in the combustion exhaust gas 21 in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas of the present embodiment is recovered by cooling the CO 2 pressurized by the second compressor 4 ′ at the subsequent stage with the cooler 5 ′. Then, the liquefied CO 2 is recovered from the cooler 5 ′, and the non-condensable gas 24 of the combustion exhaust gas 21 that is not liquefied is separated from the CO 2 23 liquefied by the cooler 5 ′ and is caused to flow downstream.
　本実施例によれば、前記金属水銀吸着塔１１、１１’を前段の圧縮機４による加圧によって温度が高くなった領域に並列に配設させた構成なので、この金属水銀吸着塔１１、１１’に流入する燃焼排ガス２１の温度が高くなり、燃焼排ガス２１中のＨｇ０を金属水銀吸着塔１１、１１’の金属水銀吸着剤に吸着させてアマルガムを更に形成し易くできる。 According to the present embodiment, the metal mercury adsorption towers 11 and 11 ′ are arranged in parallel in a region where the temperature is increased by pressurization by the compressor 4 in the previous stage. The temperature of the combustion exhaust gas 21 flowing into 'becomes high, and Hg 0 in the combustion exhaust gas 21 can be adsorbed to the metal mercury adsorbent of the metal mercury adsorption towers 11 and 11' to further easily form the amalgam.
　ところで、上記した本発明の各実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムでは、前記金属水銀吸着塔１１、１１’の内部に積層されて燃焼排ガス２１中のＨｇ０を吸着して除去する金属水銀吸着剤を長時間使用すると、金属水銀吸着剤を構成するＮｉ等の遷移金属がＨｇ０と結合して形成されるアマルガムの生成が飽和に近づいてＨｇ０の吸着性能が低下するので、定期的な金属水銀吸着剤の交換が必要になる。 Meanwhile, in the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas is the embodiment of the present invention described above, adsorbs Hg 0 in the combustion exhaust gas 21 are stacked inside the metallic mercury adsorption tower 11, 11 ' When the metal mercury adsorbent to be removed is used for a long time, the formation of amalgam formed by combining transition metals such as Ni constituting the metal mercury adsorbent with Hg 0 is close to saturation, and the adsorption performance of Hg 0 is improved. It will be necessary to replace the metal mercury adsorbent regularly.
　図１、図５～図７の各実施例で燃焼排ガス中の二酸化炭素回収設備の水銀除去システムに示したように、金属水銀ガス吸着塔１１、１１は複数個並列に設置することが望ましい。 As shown in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas in each embodiment of FIGS. 1 and 5 to 7, it is desirable to install a plurality of metal mercury gas adsorption towers 11 and 11 in parallel.
　前記したように金属水銀吸着塔１１、１１’を並列に配設することにより、燃焼排ガス２１中のＨｇ０を吸着する吸着性能が低下した金属水銀吸着剤を備えた金属水銀ガス吸着塔１１、１１’の内の一方から、新しい金属水銀吸着剤に交換して待機中の他方の金属水銀ガス吸着塔１１、１１’の内の他方に切り替えて燃焼排ガス２１を通気することで、燃焼排ガス２１中の金属水銀の除去を高い除去効率で継続して行うことができる。 As described above, by arranging the metal mercury adsorption towers 11 and 11 ′ in parallel, the metal mercury gas adsorption tower 11 having the metal mercury adsorbent having reduced adsorption performance for adsorbing Hg 0 in the combustion exhaust gas 21, The exhaust gas 21 is ventilated by switching from one of the 11 'to a new metal mercury adsorbent and switching to the other of the other metal mercury gas adsorption towers 11 and 11' waiting. The metal mercury in the inside can be continuously removed with high removal efficiency.
　また、処理すべき燃焼排ガス２１中の金属水銀の濃度が高くなり、並列に配設させた金属水銀ガス吸着塔１１、１１’に備えた金属水銀吸着剤だけでは金属水銀を除去する処理能力が不足する場合には、金属水銀を除去する処理能力を増加させるために運転中の金属水銀ガス吸着塔に加えて待機中の金属水銀ガス吸着塔が２基以上となるように予め設置しておき、３基以上の金属水銀ガス吸着塔を本実施例である燃焼排ガス中の二酸化炭素回収設備における水銀除去システムに備えた構成にすれば、燃焼排ガス２１中の金属水銀濃度が並列に配設させた２基の金属水銀ガス吸着塔の処理能力を越えて急に増加したとしても対応することが容易となる。 In addition, the concentration of metallic mercury in the combustion exhaust gas 21 to be treated becomes high, and the processing ability to remove metallic mercury is possible only with the metallic mercury adsorbent provided in the metallic mercury gas adsorption towers 11 and 11 'arranged in parallel. If there is a shortage, in order to increase the treatment capacity to remove metallic mercury, in addition to the working metallic mercury gas adsorption tower, there should be two or more standby metallic mercury gas adsorption towers in advance. If three or more metal mercury gas adsorption towers are provided in the mercury removal system in the carbon dioxide recovery facility for combustion exhaust gas according to this embodiment, the metal mercury concentration in the combustion exhaust gas 21 is arranged in parallel. In addition, it becomes easy to cope with a sudden increase beyond the processing capacity of the two metal mercury gas adsorption towers.
　次に図１、図５～図７に示した各実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムの運転方法について説明する。 Next, the operation method of the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas which is each embodiment shown in FIGS. 1 and 5 to 7 will be described.
　上記各実施例の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムに設置された制御装置１２で制御される並列に配設した各金属水銀ガス吸着塔１１の運転方法について説明する。 The operation method of the metal mercury gas adsorption towers 11 arranged in parallel controlled by the control device 12 installed in the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas of each of the above embodiments will be described.
　図８は本発明の上記した実施例に並列に配設された金属水銀ガス吸着塔１１を模式的に示したものであり、燃焼排ガス２１が通気される並列に複数個設置された金属水銀ガス吸着塔１１と、入口バルブ１３と、出口バルブ１４、及び水銀分析計１５を記号表記して模式的に示したものである。 FIG. 8 schematically shows a metal mercury gas adsorption tower 11 arranged in parallel in the above-described embodiment of the present invention, and a plurality of metal mercury gases installed in parallel through which the combustion exhaust gas 21 is vented. The adsorption tower 11, the inlet valve 13, the outlet valve 14, and the mercury analyzer 15 are schematically shown as symbols.
　図８において、金属水銀ガス吸着塔１１はｎ個（ｎ≧３）並列に設置されており、これらの金属水銀ガス吸着塔１１をＢ１からＢｎで表記する。 In FIG. 8, n (n ≧ 3) metal mercury gas adsorption towers 11 are arranged in parallel, and these metal mercury gas adsorption towers 11 are denoted by B 1 to B n .
　Ｂ１からＢｎで表記した金属水銀ガス吸着塔１１に対応させて、その上流側に設置された入口バルブ１３をＶＩ１からＶＩｎで、下流側に設置された出口バルブ１４をＶＯ１からＶＯｎで、出口バルブ１４の下流側に位置する水銀分析計１５をＳ１からＳｎで表記する。また、出口バルブ１４の後流側で合流した流路に位置する水銀分析計１５ｂをＳｅで表記する。 Corresponding to the metal mercury gas adsorption towers 11 denoted by B 1 to B n , the inlet valve 13 installed on the upstream side is connected to VI 1 to VI n and the outlet valve 14 installed on the downstream side is connected to VO 1. The mercury analyzer 15 located downstream of the outlet valve 14 is denoted by S 1 to S n as VO n . Further, denoted mercury analyzer 15b located in the flow path which is merged with the downstream side of the outlet valve 14 in S e.
　図９は本発明の上記実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムに、例えば並列に３基設置された構成の金属水銀ガス吸着塔の状態を初期設定する方法を示すフローチャートである。 FIG. 9 is a flowchart showing a method for initializing the state of a metal mercury gas adsorption tower having a configuration in which, for example, three units are installed in parallel in the mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas according to the above-described embodiment of the present invention. It is.
　図９において、「金属水銀ガス吸着塔の設定」では、その設定値Ｂｉの初期設定値として３基の各金属水銀ガス吸着塔１１について各運転状態に合わせて、手動入力で前記設定値Ｂｉをそれぞれ設定する。 In FIG. 9, in “setting of the metal mercury gas adsorption tower”, as an initial set value of the set value B i , the set value B is manually input according to each operation state of the three metal mercury gas adsorption towers 11. Set i respectively.
　例えば、１基の金属水銀ガス吸着塔１１が燃焼排ガス２１を通気中であれば、「金属水銀ガス吸着塔の設定」にて初期設定として通気中の設定値Ｂｉ＝２を設定し、他の１基の金属水銀ガス吸着塔１１が燃焼排ガス２１を通気せずに待機中であれば、初期設定として待機中の設定値Ｂｉ＝１を設定し、残りの１基の金属水銀ガス吸着塔１１が燃焼排ガス２１を通気せず且つ内部に積層した金属水銀吸着剤を新しい金属水銀吸着剤に交換中であれば、初期設定として交換中の設定値Ｂｉ＝０を設定する。 For example, if one metal mercury gas adsorption tower 11 is ventilating the combustion exhaust gas 21, the setting value B i = 2 during ventilation is set as an initial setting in “Setting of the metal mercury gas adsorption tower”, and the other If one of the metal mercury gas adsorption towers 11 is on standby without passing the flue gas 21, the initial set value B i = 1 is set as the initial setting, and the remaining one metal mercury gas adsorption is performed. If the tower 11 does not allow the flue gas 21 to pass through and the metal mercury adsorbent stacked inside is being replaced with a new metal mercury adsorbent, the set value B i = 0 during replacement is set as an initial setting.
　ここで、初期設定した設定値Ｂｉ＝０は、金属水銀吸着剤を交換中の金属水銀ガス吸着塔１１に該当することから、図９の右側に示したように、「バルブの開閉状態の設定」にて、必然的に当該金属水銀ガス吸着塔１１の入口バルブ１３と出口バルブ１４とがそれぞれ閉のＶＩｉ＝０、ＶＯｉ＝０となるように制御する機能が、前記制御装置１２に備えられている。 Here, since the initially set value B i = 0 corresponds to the metal mercury gas adsorption tower 11 in which the metal mercury adsorbent is being replaced, as shown on the right side of FIG. The function of controlling the inlet valve 13 and the outlet valve 14 of the metal mercury gas adsorption tower 11 to be closed VI i = 0 and VO i = 0, respectively, in the “setting” is necessarily the control device 12. Is provided.
　例えば、金属水銀吸着剤の交換では、金属水銀ガス吸着塔１１を開放して前記金属水銀吸着剤を交換することから、金属水銀ガス吸着塔１１の開放中は、当該金属水銀ガス吸着塔１１の入口バルブ１３と出口バルブ１４とがＶＩｉ＝０，ＶＯｉ＝０の状態から変更できないようにインターロック機能を前記制御装置１２に持たせるようにしている。 For example, when replacing the metal mercury adsorbent, the metal mercury gas adsorption tower 11 is opened and the metal mercury adsorbent is exchanged. The control device 12 is provided with an interlock function so that the inlet valve 13 and the outlet valve 14 cannot be changed from the state of VI i = 0 and VO i = 0.
　そこで前記各金属水銀ガス吸着塔１１の運転状態を、通気中、待機中、吸着剤交換中の３種類に分け、これらの３種類に分けた各金属水銀ガス吸着塔１１の運転状態をモニタ表示によって目視確認できる機能を前記制御装置１２に備えさせることが望ましく、これらの機能を制御装置１２に備えさせることによって、並列に配設された複数の金属水銀ガス吸着塔１１を稼動させながら計画的に運用することができる。 Therefore, the operation state of each metal mercury gas adsorption tower 11 is divided into three types of ventilation, standby and adsorbent exchange, and the operation state of each metal mercury gas adsorption tower 11 divided into these three types is displayed on the monitor. It is desirable to provide the control device 12 with a function that can be visually confirmed by the control device. By providing the control device 12 with these functions, a plurality of metal mercury gas adsorption towers 11 arranged in parallel can be operated systematically. Can be operated.
　そして前記した各金属水銀ガス吸着塔１１の設定値Ｂｉに合わせて、制御装置１２で各金属水銀ガス吸着塔１１に対応した入口バルブ１３及び出口バルブ１４の開閉を制御する。 And in accordance with the set value B i of each metal mercury gas adsorption tower 11 described above, controls the opening and closing of the inlet valve 13 and outlet valve 14 corresponding to each metal mercury gas adsorption tower 11 in the controller 12.
　即ち、図９の右側に示したように、「金属水銀ガス吸着塔の設定」が設定値Ｂｉ＝２の金属水銀ガス吸着塔１１であれば、「バルブの開閉状態の設定」にて当該金属水銀ガス吸着塔１１の入口バルブ１３及び出口バルブ１４はＶＩｉ＝１、ＶＯｉ＝１となるように制御装置１２で開制御する。 That is, as shown on the right side of FIG. 9, if “setting of the metal mercury gas adsorption tower” is the metal mercury gas adsorption tower 11 with the setting value B i = 2, the “setting of the valve open / close state” The inlet valve 13 and the outlet valve 14 of the metal mercury gas adsorption tower 11 are controlled to open by the control device 12 so that VI i = 1 and VO i = 1.
　また、「金属水銀ガス吸着塔の設定」が設定値Ｂｉ＝０、あるいは設定値Ｂｉ＝１の金属水銀ガス吸着塔１１であれば、「バルブの開閉状態の設定」にて当該金属水銀ガス吸着塔１１の入口バルブ１３及び出口バルブ１４はＶＩｉ＝０、ＶＯｉ＝０となるように制御装置１２で閉制御を行う。 Further, if “setting of the metal mercury gas adsorption tower” is the metal mercury gas adsorption tower 11 having the setting value B i = 0 or the setting value B i = 1, the “metal mercury gas adsorption tower 11” is set in “setting of the valve open / close state”. The inlet valve 13 and the outlet valve 14 of the gas adsorption tower 11 are closed and controlled by the control device 12 so that VI i = 0 and VO i = 0.
　上記したように、各金属水銀ガス吸着塔１１の運転状態に合わせて当該金属水銀ガス吸着塔１１の入口バルブ１３及び出口バルブ１４の開閉を自動的に制御する機能、あるいは確認制御する機能を、制御装置１２に備えておくことが望ましい。 As described above, the function of automatically controlling the opening and closing of the inlet valve 13 and the outlet valve 14 of the metal mercury gas adsorption tower 11 in accordance with the operating state of each metal mercury gas adsorption tower 11 or the function of confirming control, It is desirable that the controller 12 be provided.
　次に図１、図５～図７に示した各実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおける運転方法について、図１０のフローチャートを用いて説明する。 Next, the operation method in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas which is each embodiment shown in FIGS. 1 and 5 to 7 will be described with reference to the flowchart of FIG.
　図１０は上記した本実施例である燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、並列に配設された金属水銀ガス吸着塔１１の運転を切り替えて制御する方法を示すフローチャートである。 FIG. 10 is a flowchart showing a method for switching and controlling the operation of the metal mercury gas adsorption tower 11 arranged in parallel in the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas according to this embodiment.
　図１０において、このフローチャートにおける上限値の水銀濃度設定のステップ１０１では、制御装置１２によって各金属水銀ガス吸着塔１１に対して予め設定しておく燃焼排ガス２１中の水銀濃度の上限値ＣｒＨｇを設定する。 In FIG. 10, in the upper limit mercury concentration setting step 101 in this flowchart, the upper limit value Cr Hg of the mercury concentration in the combustion exhaust gas 21 preset by the control device 12 for each metal mercury gas adsorption tower 11 is set. Set.
　次に金属水銀ガス吸着塔１１の運転状態設定のステップ１０２では、本実施例の水銀除去システムに設置された前記金属水銀ガス吸着塔１１の基数i（i＝１～ｎ）について、複数基設置された金属水銀ガス吸着塔１１の中から燃焼排ガス２１が通気中（Ｂｉ＝２）に該当する金属水銀ガス吸着塔１１を探索し、探索した当該金属水銀ガス吸着塔１１の運転状態の設定値Ｂｉを通気中（Ｂｉ＝２）に設定する。 Next, in step 102 for setting the operating state of the metal mercury gas adsorption tower 11, a plurality of bases i (i = 1 to n) of the metal mercury gas adsorption tower 11 installed in the mercury removal system of this embodiment are installed. The metal mercury gas adsorption tower 11 corresponding to the exhaust gas 21 being ventilated (B i = 2) is searched from the metal mercury gas adsorption tower 11 thus set, and the operation state of the found metal mercury gas adsorption tower 11 is set. Set the value B i to venting (B i = 2).
　次に運転状態Ｂｉを通気中（Ｂｉ＝２）に設定した当該金属水銀ガス吸着塔１１に関して水銀濃度計測のステップ１０３に進み、当該金属水銀ガス吸着塔１１の下流側に設置した水銀分析計１５によって該金属水銀ガス吸着塔１１を流下した燃焼排ガス２１中の水銀濃度ＣＨｇ，ｉを計測する。 Next, the mercury concentration measurement step 103 is performed for the metal mercury gas adsorption tower 11 in which the operating state B i is set to be ventilated (B i = 2), and mercury analysis installed downstream of the metal mercury gas adsorption tower 11 is performed. The mercury concentration C Hg, i in the combustion exhaust gas 21 flowing down the metal mercury gas adsorption tower 11 is measured by a total 15.
　水銀分析計１５によって燃焼排ガス２１中の水銀濃度ＣＨｇ，ｉを計測すると、次に水銀濃度の比較のステップ１０４に進み、通気中（Ｂｉ＝２）の金属水銀ガス吸着塔１１に関して水銀分析計１５で計測された燃焼排ガス２１中の水銀濃度の計測値ＣＨｇ，ｉと、水銀濃度設定のステップ１０１で設定した水銀濃度の上限値ＣｒＨｇとの比較を行う。 When the mercury concentration C Hg, i in the combustion exhaust gas 21 is measured by the mercury analyzer 15, the process proceeds to the mercury concentration comparison step 104, where mercury analysis is performed on the metal mercury gas adsorption tower 11 that is ventilated (B i = 2). The measured value C Hg, i of the mercury concentration in the combustion exhaust gas 21 measured by the total 15 is compared with the upper limit value Cr Hg of the mercury concentration set in step 101 for setting the mercury concentration.
　この水銀濃度設定のステップ１０１での水銀濃度の比較において、水銀濃度の計測値ＣＨｇ，ｉ　＜　上限値ＣｒＨｇの関係であれば、探索された当該金属水銀ガス吸着塔１１は運転を継続しても問題が無いので、当該金属水銀ガス吸着塔１１の運転を継続する。 In the comparison of the mercury concentration in the mercury concentration setting step 101, if the relationship of the measured value C Hg, i <the upper limit value Cr Hg of the mercury concentration, the searched metal mercury gas adsorption tower 11 continues to operate. However, since there is no problem, the operation of the metal mercury gas adsorption tower 11 is continued.
　そして、再度、金属水銀ガス吸着塔１１の運転状態設定のステップ１０２に戻って、複数基設置された金属水銀ガス吸着塔１１の中から当該金属水銀ガス吸着塔１１以外で燃焼排ガス２１が通気中（Ｂｉ＝２）に該当する運転状態の設定値Ｂｉの金属水銀ガス吸着塔１１の探索を行って上述したものと同様の運転を行うことを繰り返す。 Then, the process returns to step 102 for setting the operating state of the metal mercury gas adsorption tower 11 again, and the combustion exhaust gas 21 is ventilating from a plurality of the metal mercury gas adsorption towers 11 other than the metal mercury gas adsorption tower 11. The search for the metal mercury gas adsorption tower 11 of the set value B i of the operation state corresponding to (B i = 2) is repeated to perform the same operation as described above.
　一方、この水銀濃度の比較のステップ１０４における水銀濃度の比較において、水銀濃度の計測値ＣＨｇ，ｉ　≧　上限値ＣｒＨｇの関係になっていれば当該金属水銀ガス吸着塔１１は運転を継続すると問題があることを示しているので、次に、運転状態が待機中を探索するステップ１０５に進み、制御装置１２によって複数基設置された金属水銀ガス吸着塔１１の中から運転状態の設定値Ｂｊが、新しい金属水銀吸着剤に入れ替えて待機中（Ｂｊ＝１）に該当する金属水銀ガス吸着塔１１を探索する。 On the other hand, in the mercury concentration comparison in the mercury concentration comparison step 104, if the relationship of the measured value C Hg, i ≧ the upper limit value Cr Hg of the mercury concentration is satisfied , the metal mercury gas adsorption tower 11 will continue to operate. Since it indicates that there is a problem, the process next proceeds to step 105 where the operating state is searched for waiting, and the operating state set value B is selected from the plurality of metal mercury gas adsorption towers 11 installed by the control device 12. j searches for a metal mercury gas adsorption tower 11 corresponding to a standby state (B j = 1) by replacing with a new metal mercury adsorbent.
　ここで、運転状態Ｂｊが待機中（Ｂｊ＝１）の金属水銀ガス吸着塔１１が複数基待機しているのであれば、制御装置１２によってこれらの中から何れか１基の金属水銀ガス吸着塔１１を手動選択しても良い。 Here, if a plurality of the metal mercury gas adsorption towers 11 whose operation state B j is on standby (B j = 1) are on standby, any one of them is controlled by the control device 12. The adsorption tower 11 may be manually selected.
　そして運転状態が待機中を探索するステップ１０５にて探索した待機中（Ｂｊ＝１）の金属水銀吸着塔１１に対して燃焼排ガス２１の通気を行うように、次の運転状態変更及びバルブ操作のステップ１０６に進み、制御装置１２によって当該金属水銀吸着塔１１の運転状態Ｂｉを待機中（Ｂｊ＝１）から通気中（Ｂｉ＝２）に変更し、通気中（Ｂｉ＝２）の運転状態に変更されたこの金属水銀吸着塔１１の入口バルブ１３及び出口バルブ１４とをそれぞれ開のＶＩｊ＝１、ＶＯｊ＝１となるように制御して、燃焼排ガス２１をこの金属水銀吸着塔１１に通気させる。 Then, the next operation state change and valve operation are performed so that the flue gas 21 is vented to the metal mercury adsorption tower 11 in the standby state (B j = 1) searched in Step 105 in which the operation state is searched for standby. , The control device 12 changes the operating state B i of the metal mercury adsorption tower 11 from waiting (B j = 1) to venting (B i = 2), and venting (B i = 2). ), The inlet valve 13 and the outlet valve 14 of the metal mercury adsorption tower 11 changed to the operating state are controlled so that VI j = 1 and VO j = 1 are opened, respectively. The mercury adsorption tower 11 is vented.
　また、複数基設置された金属水銀ガス吸着塔１１のうち、水銀濃度の比較のステップ１０４における水銀濃度の比較において水銀濃度の計測値ＣＨｇ，ｉ　≧　上限値ＣｒＨｇとなり、金属水銀吸着剤によるＨｇ０の吸着性能が低下して金属水銀の吸着状態が悪くなった金属水銀ガス吸着塔１１に関しては、次の運転状態再変更及びバルブ操作のステップ１０７に進み、制御装置１２によって当該金属水銀吸着塔１１の運転状態の設定値Ｂｊを通気中（Ｂｉ＝２）から交換中（Ｂｊ＝０）に変更し、当該金属水銀ガス吸着塔１１の入口バルブ１３及び出口バルブ１４がそれぞれ閉のＶＩｉ＝０、ＶＯｉ＝０となるように制御して、当該金属水銀吸着塔１１への燃焼排ガス２１の通気を遮断する。 In addition, among the metal mercury gas adsorption towers 11 installed in a plurality of units, the mercury concentration measurement value C Hg, i ≧ the upper limit value Cr Hg in the mercury concentration comparison in the mercury concentration comparison step 104, which depends on the metal mercury adsorbent. With respect to the metal mercury gas adsorption tower 11 in which the adsorption performance of Hg 0 is deteriorated and the adsorption state of the metal mercury is deteriorated, the operation proceeds to the next operation state re-change and valve operation step 107, and the control device 12 performs the metal mercury adsorption. The set value B j of the operation state of the tower 11 is changed from being ventilated (B i = 2) to being exchanged (B j = 0), and the inlet valve 13 and the outlet valve 14 of the metal mercury gas adsorption tower 11 are closed. In this way, the ventilation of the combustion exhaust gas 21 to the metal mercury adsorption tower 11 is blocked by controlling so that VI i = 0 and VO i = 0.
　そして燃焼排ガス２１の通気を遮断後に、当該金属水銀吸着塔１１における金属水銀吸着剤を新しい金属水銀吸着剤に入れ替え、当該金属水銀吸着塔１１が燃焼排ガス２１の通気の待機状態になった場合に、再度、運転状態が待機中を探索するステップ１０５に戻って、制御装置１２によってこの待機状態の金属水銀ガス吸着塔１１の運転状態の設定Ｂｉを、交換中（Ｂｉ＝０）から待機中（Ｂｉ＝１）に修正すればよい。 Then, after the ventilation of the combustion exhaust gas 21 is interrupted, the metal mercury adsorption agent in the metal mercury adsorption tower 11 is replaced with a new metal mercury adsorption agent, and the metal mercury adsorption tower 11 enters a standby state for the ventilation of the combustion exhaust gas 21. Returning to step 105 where the operating state is waiting again, the control device 12 sets the standby state B i of the metal mercury gas adsorption tower 11 in the standby state from being replaced (B i = 0) to standby. It may be corrected to medium (B i = 1).
　このように、各金属水銀吸着塔１１を流下した燃焼排ガス２１中の水銀濃度の上限値ＣｒＨｇと水銀分析計１５で計測された計測値ＣＨｇ，ｉとを比較する機能、金属水銀吸着剤が性能低下したことを知らせる機能、金属水銀吸着剤を交換すべき金属水銀ガス吸着塔１１を探索する機能を、制御装置１２に備えておくことが望ましい。 Thus, the function of comparing the upper limit value Cr Hg of the mercury concentration in the combustion exhaust gas 21 flowing down each metal mercury adsorption tower 11 with the measured value C Hg, i measured by the mercury analyzer 15, the metal mercury adsorbent It is desirable to provide the control device 12 with a function of notifying that the performance has deteriorated and a function of searching for the metal mercury gas adsorption tower 11 whose metal mercury adsorbent should be replaced.
　図１１は本実施例である燃焼排ガス中の二酸化炭素回収設備における水銀除去システムに並列に配設された複数基の金属水銀ガス吸着塔１１の運転を追加制御する方法を示すフローチャートである。 FIG. 11 is a flowchart showing a method for additionally controlling the operation of a plurality of metal mercury gas adsorption towers 11 arranged in parallel to the mercury removal system in the carbon dioxide recovery facility for combustion exhaust gas according to this embodiment.
　図１１において、このフローチャートにおける水銀濃度上限値設定のステップ２０１では、制御装置１２によって複数基設置された金属水銀ガス吸着塔１１の下流側の燃焼排ガス２１の流路集合部における水銀濃度として、複数基設置された金属水銀ガス吸着塔１１の全体としての燃焼排ガス２１に対して予め設定する燃焼排ガス２１中の水銀濃度の上限値ＣｒＨｇ，ｅを設定する。 In FIG. 11, in the step 201 for setting the mercury concentration upper limit value in this flowchart, a plurality of mercury concentrations are set in the flow path assembly portion of the combustion exhaust gas 21 on the downstream side of the metallic mercury gas adsorption tower 11 installed by the control device 12. An upper limit value Cr Hg, e of the mercury concentration in the combustion exhaust gas 21 set in advance for the combustion exhaust gas 21 as the whole of the metal mercury gas adsorption tower 11 installed in the base is set.
　次に複数基設置された金属水銀ガス吸着塔１１に関して水銀濃度計測のステップ２０３に進み、これら複数基の金属水銀ガス吸着塔１１の下流側の流路集合部に設けた水銀分析計１５ｂによって複数基設置された金属水銀ガス吸着塔１１を流下した燃焼排ガス２１中の水銀濃度ＣＨｇ，ｅを計測する。 Next, the process proceeds to step 203 for measuring the mercury concentration with respect to the plurality of metal mercury gas adsorption towers 11 installed, and a plurality of mercury mercury analyzers 15b provided at the flow path assembly on the downstream side of the plurality of metal mercury gas adsorption towers 11 are used. The mercury concentration C Hg, e in the combustion exhaust gas 21 flowing down the metal mercury gas adsorption tower 11 installed in the base is measured.
　水銀分析計１５ｂによって流路集合部での燃焼排ガス２１中の水銀濃度ＣＨｇ，ｅを計測すると、次に水銀濃度の比較のステップ２０４に進み、金属水銀ガス吸着塔１１に関して流路集合部の水銀分析計１５ｂで計測された燃焼排ガス２１中の水銀濃度の計測値、ＣＨｇ，ｅと、水銀濃度上限値設定のステップ２０１で設定した水銀濃度の上限値ＣｒＨｇ，ｅとの比較を行う。 When the mercury concentration C Hg, e in the combustion exhaust gas 21 at the flow passage assembly portion is measured by the mercury analyzer 15b, the process proceeds to the next step 204 for comparing the mercury concentration, and the flow rate collection portion of the metal mercury gas adsorption tower 11 is measured. The measurement value of mercury concentration in combustion exhaust gas 21 measured by the mercury analyzer 15b, C Hg, e, is compared with the upper limit value Cr Hg, e of the mercury concentration set in step 201 for setting the mercury concentration upper limit value. .
　この水銀濃度の比較のステップ２０４での水銀濃度の比較において、水銀濃度の計測値ＣＨｇ，ｅ　＜　上限値ＣｒＨｇ，ｅの関係であれば、複数基設置された金属水銀ガス吸着塔１１の全体としての燃焼排ガス２１の水銀濃度の計測値ＣＨｇ，ｅが上限値ＣｒＨｇ，ｅの制限範囲内であるので、複数基設置されたこれらの金属水銀ガス吸着塔１１の現状の運転状態を継続させる。 In the comparison of the mercury concentration in the mercury concentration comparison step 204, if the relationship of the measured value C Hg, e <the upper limit value Cr Hg, e of the mercury concentration, a plurality of metal mercury gas adsorption towers 11 installed. Since the measured value C Hg, e of the mercury concentration of the combustion exhaust gas 21 as a whole is within the limit range of the upper limit value Cr Hg, e , the current operation state of the plurality of these metal mercury gas adsorption towers 11 installed is determined. Let it continue.
　そして、前記金属水銀ガス吸着塔１１の現状の運転状態の継続中に再度、複数基設置された金属水銀ガス吸着塔１１に関する水銀濃度計測のステップ２０３に戻って、金属水銀ガス吸着塔１１の下流側の流路集合部での水銀分析計１５ｂによって複数基設置された金属水銀ガス吸着塔１１を流下した燃焼排ガス２１中の水銀濃度ＣＨｇ，ｅの計測を継続する。 Then, while continuing the current operation state of the metal mercury gas adsorption tower 11, the process returns to the step 203 for measuring the mercury concentration related to the plurality of metal mercury gas adsorption towers 11 installed downstream of the metal mercury gas adsorption tower 11. The measurement of the mercury concentration C Hg, e in the combustion exhaust gas 21 flowing down the metal mercury gas adsorption tower 11 installed in a plurality by the mercury analyzer 15b at the flow path collecting portion on the side is continued.
　一方、この水銀濃度の比較のステップ２０４における水銀濃度の比較において、水銀濃度の計測値ＣＨｇ，ｅ≧　ＣｒＨｇ，ｅの関係になっていれば、燃焼排ガス２１を通気している金属水銀ガス吸着塔１１を含んだ複数基設置された金属水銀ガス吸着塔１１の中に運転を継続すると問題がある別の金属水銀ガス吸着塔１１が存在していることを示している。 On the other hand, in the mercury concentration comparison in the mercury concentration comparison step 204, if the measured mercury concentration value C Hg, e ≧ Cr Hg, e is satisfied, the metal mercury gas flowing through the combustion exhaust gas 21 is used. This shows that there is another metal mercury gas adsorption tower 11 which has a problem when the operation is continued in the metal mercury gas adsorption tower 11 provided with a plurality of units including the adsorption tower 11.
　よって、新たに燃焼排ガス２１を追加して通気すべき金属水銀ガス吸着塔１１を選定するために、次に、運転状態が待機中を探索するステップ２０５に進み、制御装置１２によって複数基設置された金属水銀ガス吸着塔１１の中から運転状態の設定値Ｂｊが、新しい金属水銀吸着剤に入れ替えて待機中（Ｂｊ＝１）である金属水銀ガス吸着塔１１を探索する。 Therefore, in order to newly select the metal mercury gas adsorption tower 11 to which the flue gas 21 is to be added and to be ventilated, the process proceeds to step 205 in which the operating state is searched for waiting, and a plurality of units are installed by the control device 12. The metal mercury gas adsorption tower 11 in which the set value B j of the operation state is replaced with a new metal mercury adsorbent and is on standby (B j = 1) is searched from the metal mercury gas adsorption tower 11.
　ここで、運転状態Ｂｊが待機中（Ｂｊ＝１）の金属水銀ガス吸着塔１１が複数基待機しているのであれば、制御装置１２によってこれらの中から何れか１基の金属水銀ガス吸着塔１１を手動で選択しても良い。 Here, if a plurality of the metal mercury gas adsorption towers 11 whose operation state B j is on standby (B j = 1) are on standby, any one of them is controlled by the control device 12. The adsorption tower 11 may be selected manually.
　そして運転状態が待機中を探索するステップ２０５にて探索した待機中（Ｂｊ＝１）の当該金属水銀吸着塔１１に対して燃焼排ガス２１の通気を追加して行うことができるように、次の運転状態変更及びバルブ操作のステップ２０６に進み、制御装置１２によって当該金属水銀吸着塔１１の運転状態Ｂｉを待機中（Ｂｊ＝１）から通気中（Ｂｉ＝２）に変更し、通気中（Ｂｉ＝２）の運転状態に変更された当該金属水銀吸着塔１１の入口バルブ１３及び出口バルブ１４とをそれぞれ開のＶＩｊ＝１、ＶＯｊ＝１となるように制御して、燃焼排ガス２１をこの追加させた当該金属水銀吸着塔１１に通気させる。 Then, in order to be able to perform additional ventilation of the combustion exhaust gas 21 to the metal mercury adsorption tower 11 in the standby (B j = 1) searched in step 205 for searching for the standby in the operating state, The operation state change and the valve operation step 206 are proceeded to, and the control device 12 changes the operation state B i of the metal mercury adsorption tower 11 from waiting (B j = 1) to venting (B i = 2), The inlet valve 13 and the outlet valve 14 of the metal mercury adsorption tower 11 changed to the operating state during ventilation (B i = 2) are controlled so as to be open VI j = 1 and VO j = 1, respectively. Then, the flue gas 21 is passed through the added metal mercury adsorption tower 11.
　このように複数基設置された金属水銀ガス吸着塔１１の下流側の流路集合部に設けた水銀分析計１５ｂによって全体としての燃焼排ガス２１中の水銀濃度を計測することにより、金属水銀ガス吸着塔１１の下流側の流路集合部で計測された全体としての水銀濃度に応じて燃焼排ガス２１中の金属水銀を吸着して除去する金属水銀ガス吸着塔１１の運転台数を追加して燃焼排ガス２１を通気させる運転を行うことが可能となる。 The mercury concentration in the combustion exhaust gas 21 as a whole is measured by the mercury analyzer 15b provided in the flow passage assembly on the downstream side of the metal mercury gas adsorption tower 11 installed in plural in this way, thereby the metal mercury gas adsorption. Combustion exhaust gas by adding an operating number of metal mercury gas adsorption towers 11 for adsorbing and removing metal mercury in the combustion exhaust gas 21 according to the mercury concentration as a whole measured at the flow path gathering portion on the downstream side of the tower 11 It is possible to perform an operation of venting 21.
　上記したように本発明の各実施例によれば、燃焼排ガス中からＣＯ２を回収すると共に、燃焼排ガス中に含まれたＨｇ０を高精度で除去することを可能にした燃焼排ガス中の二酸化炭素回収設備の水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法が実現できる。 As described above, according to the embodiments of the present invention, CO 2 is recovered from the combustion exhaust gas, and Hg 0 contained in the combustion exhaust gas can be removed with high accuracy. A mercury removal system for carbon recovery equipment and a mercury removal operation method for carbon dioxide recovery equipment in combustion exhaust gas can be realized.
　また、本発明の実施例では、金属水銀吸着剤を内部に設置した金属水銀ガス吸着塔を並列に複数基配設したことにより、燃焼排ガス中から二酸化炭素を回収するために該燃焼排ガス中の二酸化炭素を液化する圧縮機に供給される燃焼排ガス中から金属水銀を高精度で除去することが可能となる。 Further, in the embodiment of the present invention, by arranging a plurality of metal mercury gas adsorption towers with metal mercury adsorbents installed in parallel, in order to recover carbon dioxide from the combustion exhaust gas, Metallic mercury can be removed with high accuracy from the combustion exhaust gas supplied to the compressor that liquefies carbon dioxide.
　この結果、本実施例では燃焼排ガス中の金属水銀を高精度で除去できるので、燃焼排ガス中の二酸化炭素を液化する圧縮機を構成する部材が腐食することなく、圧縮機を長時間稼動することができる。 As a result, in this embodiment, the metal mercury in the combustion exhaust gas can be removed with high accuracy, so that the member constituting the compressor that liquefies carbon dioxide in the combustion exhaust gas can be operated for a long time without corrosion. Can do.
　本発明は、燃焼排ガス中の二酸化炭素回収設備における水銀除去システム、及び燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法に適用可能である。 The present invention is applicable to a mercury removal system in a carbon dioxide recovery facility in combustion exhaust gas and a mercury removal operation method of the carbon dioxide recovery facility in combustion exhaust gas.

Claims (15)

  1. 　燃焼排ガスの発生源から排出された燃焼排ガス中の水分を除去する脱水装置と、この脱水装置の下流側に設置されて水分を除去した該燃焼排ガス中の二酸化炭素を圧縮する圧縮機及び圧縮された二酸化炭素を冷却して液化する冷却器を有する燃焼排ガス中の二酸化炭素回収設備とを備え、前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に燃焼排ガス中の水銀を吸着して除去する水銀ガス吸着塔を並列に複数基配設したことを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。 A dehydrator for removing moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas, a compressor for compressing carbon dioxide in the combustion exhaust gas that is installed downstream of the dehydrator and removes moisture, and And a carbon dioxide recovery facility in the combustion exhaust gas having a cooler that cools and liquefies the carbon dioxide, and the mercury in the combustion exhaust gas is upstream of the dehydration device or between the dehydration device and the compressor. A mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, comprising a plurality of mercury gas adsorption towers arranged in parallel for adsorption and removal.
  2. 　燃焼排ガスの発生源から排出された燃焼排ガス中の水分を除去する脱水装置と、この脱水装置の下流側に設置されて水分を除去した該燃焼排ガス中の二酸化炭素を圧縮する圧縮機及び圧縮された二酸化炭素を冷却して液化する冷却器を有する燃焼排ガス中の二酸化炭素回収設備とを備え、前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に燃焼排ガス中の水銀を吸着して除去する水銀ガス吸着塔を並列に複数基配設し、複数基設配設された各水銀ガス吸着塔の上流側及び下流側に燃焼排ガスの流通を調節する入口バルブ及び出口バルブをそれぞれ設置し、前記出口バルブの下流側に燃焼排ガス中の水銀濃度を計測する水銀分析計を設置し、前記水銀分析計で計測した燃焼排ガス中の水銀濃度に基づいて前記水銀ガス吸着塔の入口バルブ及び出口バルブの開閉を制御する制御装置を設置したことを特徴とする燃焼排ガス中の二酸化炭素回収の水銀除去システム。 A dehydrator for removing moisture in the combustion exhaust gas discharged from the source of combustion exhaust gas, a compressor for compressing carbon dioxide in the combustion exhaust gas that is installed downstream of the dehydrator and removes moisture, and And a carbon dioxide recovery facility in the combustion exhaust gas having a cooler that cools and liquefies the carbon dioxide, and the mercury in the combustion exhaust gas is upstream of the dehydration device or between the dehydration device and the compressor. A plurality of mercury gas adsorption towers to be adsorbed and removed are arranged in parallel, and an inlet valve and an outlet valve for adjusting the flow of combustion exhaust gas are arranged upstream and downstream of each of the mercury gas adsorption towers arranged in plurality. A mercury analyzer that measures mercury concentration in the combustion exhaust gas is installed downstream of the outlet valve, and the mercury gas adsorption tower is based on the mercury concentration in the combustion exhaust gas measured by the mercury analyzer. Carbon dioxide recovery mercury removal system of combustion exhaust gas, characterized in that the control device is installed to control the opening and closing of the inlet valve and outlet valve.
  3. 　請求項１又は請求項２に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記脱水装置を流下した燃焼排ガスを前記圧縮機に導く燃焼ガス流路は並列に複数配設させており、これらの並列に配設された燃焼ガス流路に前記金属水銀ガス吸着塔がそれぞれ設置されていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 1 or claim 2,
    A plurality of combustion gas passages for introducing the combustion exhaust gas flowing down the dehydrator to the compressor are arranged in parallel, and the metal mercury gas adsorption tower is installed in each of the combustion gas passages arranged in parallel. A mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, characterized by
  4. 　請求項１又は請求項２に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　燃焼排ガスを前記脱水装置に導く燃焼ガス流路は並列に複数配設させており、これらの並列に配設された燃焼ガス流路に前記水銀ガス吸着塔がそれぞれ設置され、前記水銀ガス吸着塔を流下した燃焼排ガスは前記脱水装置を経由してから前記圧縮機に導かれるように構成されていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 1 or claim 2,
    A plurality of combustion gas passages for introducing combustion exhaust gas to the dehydrator are arranged in parallel, and the mercury gas adsorption tower is installed in each of the combustion gas passages arranged in parallel, and the mercury gas adsorption tower The system for removing mercury from carbon dioxide recovery equipment in combustion exhaust gas is characterized in that the combustion exhaust gas flowing down the exhaust gas is guided to the compressor after passing through the dehydrator.
  5. 　請求項１又は請求項２に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記圧縮機は上流側に設置した第１の圧縮機と、下流側に設置した第２の圧縮機から構成され、前記冷却器は第２の圧縮機の下流側に設置されており、前記脱水装置及び第１の圧縮機を順次流下した燃焼排ガスを前記第２の圧縮機に導く燃焼ガス流路は並列に配設させており、これらの並列に配設された燃焼ガス流路に前記水銀ガス吸着塔がそれぞれ設置されていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 1 or claim 2,
    The compressor is composed of a first compressor installed on the upstream side and a second compressor installed on the downstream side, and the cooler is installed on the downstream side of the second compressor. Combustion gas passages for introducing the combustion exhaust gas flowing down the apparatus and the first compressor to the second compressor are arranged in parallel, and the mercury gas is disposed in the combustion gas passages arranged in parallel. A mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, characterized in that each gas adsorption tower is installed.
  6. 　請求項５に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記並列に配設された燃焼ガス流路にそれぞれ設置された前記水銀ガス吸着塔を流下した燃焼排ガスを合流させて前記第２の圧縮機に導く前記第２の圧縮機の上流側に燃焼排ガスを冷却する第２の冷却器を設置したことを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 5,
    Combustion exhaust gas upstream of the second compressor that joins the combustion exhaust gas flowing down the mercury gas adsorption towers installed respectively in the combustion gas flow paths arranged in parallel and leads to the second compressor The mercury removal system of the carbon dioxide recovery equipment in combustion exhaust gas characterized by having installed the 2nd cooler which cools.
  7. 　請求項１乃至請求項５の何れか１項に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記水銀ガス吸着塔の内部には燃焼排ガス中の水銀を吸着する水銀吸着剤が設置され、この水銀吸着剤はニッケルを含有する合金から形成されていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery facility in the combustion exhaust gas according to any one of claims 1 to 5,
    A mercury adsorbent that adsorbs mercury in the flue gas is installed inside the mercury gas adsorption tower, and the mercury adsorbent is formed of an alloy containing nickel, and carbon dioxide in the flue gas Mercury removal system for recovery equipment.
  8. 　請求項７に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記水銀ガス吸着剤は、板状吸着剤として複数枚配設されると共に、隣接した板状吸着剤の間に燃焼排ガスを流下する流路を形成させていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 7,
    A plurality of the mercury gas adsorbents are arranged as plate-like adsorbents, and a flow path for flowing the flue gas between adjacent plate-like adsorbents is formed. Mercury removal system for carbon dioxide recovery equipment.
  9. 　請求項７に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記水銀ガス吸着剤は、ハニカム状吸着剤として燃焼排ガスを流下させる多数の空孔が形成されて配設されていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 7,
    A mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, wherein the mercury gas adsorbent is provided with a large number of holes for allowing the combustion exhaust gas to flow down as a honeycomb adsorbent.
  10. 　請求項８に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記水銀ガス吸着剤は、通電により板状吸着剤を加熱するヒータを備えていることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 8,
    The mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, wherein the mercury gas adsorbent includes a heater that heats the plate adsorbent when energized.
  11. 　請求項１乃至請求項７の何れか１項に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去システムにおいて、
    　前記燃焼排ガス中の水銀は金属水銀であり、前記水銀ガス吸着塔は燃焼排ガス中の金属水銀を吸着して除去する金属水銀ガス吸着塔であることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去システム。     In the mercury removal system of the carbon dioxide recovery equipment in the combustion exhaust gas according to any one of claims 1 to 7,
    The mercury in the combustion exhaust gas is metallic mercury, and the mercury gas adsorption tower is a metal mercury gas adsorption tower that adsorbs and removes the metal mercury in the combustion exhaust gas, and the carbon dioxide recovery equipment in the combustion exhaust gas is characterized in that Mercury removal system.
  12. 　燃焼排ガスの発生源から排出された燃焼排ガス中の水分を脱水装置によって除去し、この脱水装置で水分を除去した燃焼排ガス中の二酸化炭素を該脱水装置の下流側に設置された圧縮機によって圧縮し、圧縮された二酸化炭素を冷却器によって冷却して液化させることによって前記燃焼排ガスからこの二酸化炭素を回収する運転を行い、
    　前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に並列に複数基配設された燃焼排ガス中の水銀を吸着して除去する水銀ガス吸着塔のうち、一基の水銀ガス吸着搭に対して該脱水装置に流入する前の燃焼排ガス、あるいは該脱水装置を流下した後の燃焼排ガスを通気して前記燃焼排ガス中の水銀を除去する運転を行うと共に、前記水銀ガス吸着塔のうち、少なくとも他の１基の水銀ガス吸着搭に対して前記燃焼排ガスを通気させずに待機状態にしておくことを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法。     Moisture in the flue gas discharged from the source of flue gas is removed by a dehydrator, and carbon dioxide in the flue gas from which water has been removed by this dehydrator is compressed by a compressor installed downstream of the dehydrator. Then, the compressed carbon dioxide is cooled by a cooler and liquefied to perform an operation of recovering the carbon dioxide from the combustion exhaust gas,
    One mercury gas in a mercury gas adsorption tower that adsorbs and removes mercury in combustion exhaust gas arranged upstream in parallel with the dehydrator or between the dehydrator and the compressor. The mercury gas adsorption tower is operated so as to remove the mercury in the combustion exhaust gas by ventilating the combustion exhaust gas before flowing into the dehydration device or the combustion exhaust gas after flowing down the dehydration device with respect to the adsorption tower. A method for removing mercury from carbon dioxide recovery equipment in combustion exhaust gas, characterized in that the combustion exhaust gas is not allowed to pass through at least one other mercury gas adsorption tower and is in a standby state.
  13. 　燃焼排ガスの発生源から排出された燃焼排ガス中の水分を脱水装置によって除去し、この脱水装置で水分を除去した燃焼排ガス中の二酸化炭素を該脱水装置の下流側に設置された圧縮機によって圧縮し、圧縮された二酸化炭素を冷却器によって冷却して液化させることによって前記燃焼排ガスからこの二酸化炭素を回収する運転を行い、
    　前記脱水装置の上流側、あるいは前記脱水装置と前記圧縮機との間に並列に複数基設けた水銀ガス吸着塔によって燃焼排ガス中の水銀を吸着させて除去する際に、前記水銀ガス吸着塔を流下した燃焼排ガス中の水銀濃度に基づいてこれらの並列に複数基設設された水銀ガス吸着塔のうち、１基の水銀ガス吸着搭に対して該脱水装置に流入する前の燃焼排ガス、あるいは該脱水装置を流下した後の燃焼排ガスを通気するように制御して前記燃焼排ガス中の水銀を除去する運転を行い、
    　前記水銀ガス吸着塔を流下した燃焼排ガス中の水銀濃度が所定値に達した場合には、前記水銀ガス吸着塔のうち、燃焼排ガスを通気させずに待機状態にある少なくとも１基の水銀ガス吸着搭に対して前記燃焼排ガスを通気させるように燃焼排ガスを切り替えて通気するように制御して前記燃焼排ガス中の水銀を除去する運転を行うことを特徴とする燃焼排ガス中の二酸化炭素回収の水銀除去運転方法。     Moisture in the flue gas discharged from the source of flue gas is removed by a dehydrator, and carbon dioxide in the flue gas from which water has been removed by this dehydrator is compressed by a compressor installed downstream of the dehydrator. Then, the compressed carbon dioxide is cooled by a cooler and liquefied to perform an operation of recovering the carbon dioxide from the combustion exhaust gas,
    When the mercury in the combustion exhaust gas is adsorbed and removed by the mercury gas adsorption tower provided in a plurality in parallel between the dehydration apparatus and the compressor, the mercury gas adsorption tower is Of the mercury gas adsorption towers installed in parallel based on the mercury concentration in the flue gas flowing down, the flue gas before flowing into the dehydrator for one mercury gas adsorption tower, or Performing an operation to remove the mercury in the flue gas by controlling the flue gas after flowing down the dehydrator to vent,
    When the mercury concentration in the combustion exhaust gas flowing down the mercury gas adsorption tower reaches a predetermined value, at least one mercury gas adsorption in the standby state without passing the combustion exhaust gas out of the mercury gas adsorption tower Mercury for recovering carbon dioxide in combustion exhaust gas, characterized in that the combustion exhaust gas is controlled so as to be ventilated so that the combustion exhaust gas is ventilated to the tower, and mercury is removed from the combustion exhaust gas. Removal operation method.
  14. 　請求項１２又は請求項１３項に記載の燃焼排ガス中の二酸化炭素回収の水銀除去運転方法において、
    　並列に複数基設配設された各水銀ガス吸着塔に対する燃焼排ガスの通気、あるいは通気の待機状態の制御は、前記水銀ガス吸着塔を流下した燃焼排ガス中の水銀濃度の計測値と設定値との比較に基づいてこの水銀ガス吸着塔の上流側及び下流側にそれぞれ設置した入口バルブ及び出口バルブの開閉操作を行うことによって行うことを特徴とする燃焼排ガス中の二酸化炭素回収の水銀除去運転方法。     In the mercury removal operation method of carbon dioxide recovery in combustion exhaust gas according to claim 12 or claim 13,
    Control of the ventilation of the combustion exhaust gas to each mercury gas adsorption tower arranged in parallel in plural or the standby state of ventilation is performed by measuring and setting the mercury concentration in the combustion exhaust gas flowing down the mercury gas adsorption tower. And a mercury removal operation method for carbon dioxide recovery from combustion exhaust gas, which is performed by opening and closing an inlet valve and an outlet valve respectively installed upstream and downstream of the mercury gas adsorption tower .
  15. 　請求項１２又は請求項１３に記載の燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法において、
    　前記燃焼排ガス中の水銀は金属水銀であり、前記水銀ガス吸着塔は燃焼排ガス中の金属水銀を吸着して除去する金属水銀ガス吸着塔であることを特徴とする燃焼排ガス中の二酸化炭素回収設備の水銀除去運転方法。     In the mercury removal operation method of the carbon dioxide recovery equipment in the combustion exhaust gas according to claim 12 or claim 13,
    The mercury in the combustion exhaust gas is metallic mercury, and the mercury gas adsorption tower is a metal mercury gas adsorption tower that adsorbs and removes the metal mercury in the combustion exhaust gas, and the carbon dioxide recovery equipment in the combustion exhaust gas is characterized in that Mercury removal operation method.
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