WO2010131327A1 - Equipement pour la désulfurisation d'un gaz de combustion par de l'eau de mer et procédé de traitement de l'eau de mer utilisée lors de la désulfurisation - Google Patents

Equipement pour la désulfurisation d'un gaz de combustion par de l'eau de mer et procédé de traitement de l'eau de mer utilisée lors de la désulfurisation Download PDF

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Publication number
WO2010131327A1
WO2010131327A1 PCT/JP2009/058780 JP2009058780W WO2010131327A1 WO 2010131327 A1 WO2010131327 A1 WO 2010131327A1 JP 2009058780 W JP2009058780 W JP 2009058780W WO 2010131327 A1 WO2010131327 A1 WO 2010131327A1
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WIPO (PCT)
Prior art keywords
seawater
flue gas
gas desulfurization
mixing tank
weir
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PCT/JP2009/058780
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English (en)
Japanese (ja)
Inventor
知雄 秋山
進 沖野
英次 越智
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三菱重工業株式会社
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Application filed by 三菱重工業株式会社 filed Critical 三菱重工業株式会社
Priority to MYPI2011001306A priority Critical patent/MY170614A/en
Priority to PCT/JP2009/058780 priority patent/WO2010131327A1/fr
Priority to KR1020117007344A priority patent/KR101269707B1/ko
Priority to SA109300664A priority patent/SA109300664B1/ar
Publication of WO2010131327A1 publication Critical patent/WO2010131327A1/fr

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    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • 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
    • B01D53/14—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 by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • 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
    • B01D53/77—Liquid phase processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/101—Sulfur compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents

Definitions

  • the present invention relates to a seawater flue gas desulfurization apparatus, a seawater flue gas desulfurization system, and a method for treating desulfurized seawater, which desulfurize sulfur such as oxide sulfur in an exhaust gas from an industrial combustion facility using seawater.
  • seawater flue gas desulfurization device In a normal thermal power plant, since a large amount of seawater is used as cooling water in a boiler condenser, a part of the seawater effluent discharged from the condenser and heated is supplied to a seawater flue gas desulfurization device. The SO 2 in the exhaust gas is removed by using it as an absorbing liquid for desulfurization of seawater flue gas.
  • FIG. 9 An example of a flow diagram of a thermal power generation system provided with a seawater flue gas desulfurization device using conventional seawater is shown in FIG.
  • a thermal power generation system 100 using a conventional seawater flue gas desulfurization apparatus uses a preheated air 101 to burn with a burner (not shown), and is heat-exchanged by the boiler 102 and discharged.
  • a dust collector 104 that removes soot and dust in the exhaust gas 103, and sulfur-absorbing seawater 106 containing a high concentration of sulfur produced by desulfurizing and desulfurizing sulfur in the exhaust gas 103 using seawater 105.
  • a seawater flue gas desulfurization apparatus 107A for performing a water quality recovery process.
  • the seawater flue gas desulfurization apparatus 107A has a high concentration of a flue gas desulfurization absorption tower 108 that collects SO 2 in the exhaust gas 103 as sulfurous acid (H 2 SO 3 ), and a high concentration of sulfur content discharged from the flue gas desulfurization absorption tower 108. And an oxidation tank 109 that performs a water quality recovery process of the sulfur-absorbing seawater 106 contained in the water (Patent Documents 1 and 2).
  • Exhaust gas 103 generated by combustion in the boiler 102 is fed to a flue gas denitration device (not shown) and denitrated, and then fed to a dust collector 104 to remove the dust in the exhaust gas 103. Then, the exhaust gas 103 removed by the dust collector 104 is supplied into the exhaust gas desulfurization device 108 of the seawater exhaust gas desulfurization device 107A by the induction fan 110.
  • the sulfur content in the exhaust gas 103 is desulfurized using a part of the seawater 105A for absorption out of the seawater 105 pumped up from the sea 111. That is, the exhaust gas 103 produced by burning fossil fuel contains a sulfur content that is sulfur oxide (SO x ) in the form of SO 2 or the like.
  • SO x sulfur oxide
  • an absorption seawater 105A of the flue gas desulfurization absorber tower 108 is supplied via the exhaust gas 103 and seawater supply line 112 by gas-liquid contact, to absorb SO 2 in the flue gas 103 in the absorber seawater 105A .
  • the purified gas 113 desulfurized by the flue gas desulfurization absorption tower 108 passes through the purified gas discharge passage 114 and is released into the atmosphere from the chimney 115.
  • the reaction shown in the following formula occurs by the contact between the seawater 105A and the exhaust gas 103.
  • the gas-liquid contact between the seawater 105A and the exhaust gas 103 absorbs SO 2 in the exhaust gas 103 to generate H 2 SO 3 , which dissociates in the seawater 105A, so that the seawater 105A and the exhaust gas 103 are brought into gas-liquid contact.
  • the concentration of HSO 3 ⁇ increases, and H + is released, so that the pH decreases.
  • the pH of the sulfur-absorbing seawater 106 produced by absorbing a large amount of sulfur is about 3-6.
  • the sulfur-absorbing seawater 106 discharged from the flue gas desulfurization absorption tower 108 needs to have its pH raised to 6.0 or higher before being released or reused into the sea 111. Therefore, the sulfur-absorbing seawater 106 containing sulfur is mixed with part of the seawater 105 supplied by the secondary seawater supply line 116 in the oxidation tank 109 as dilution seawater 105B, and at the same time from the oxidizing air blower 117. Air 118 is supplied into the oxidation tank 109 through the nozzle 120 of the diffuser pipe 119 and is brought into gas-liquid contact with the sulfur-absorbing seawater to cause a reaction as shown in the following formula.
  • the sulfur-absorbing seawater 106 is discharged from a condenser (not shown) in order to prevent the diffusion of SO 2 and improve the pH in the oxidation tank 109.
  • the mixture is diluted with the seawater 105 and the oxidation tank 109 and oxidized and aerated in the oxidation tank 109 to oxidize and detoxify the sulfurous acid, increase the dissolved oxygen concentration, decarboxylate, and absorb the sulfur content.
  • the pH of the seawater drainage 122 is discharged so as to satisfy the drainage standard (usually pH 6.0 or higher) (Patent Documents 1 and 2).
  • FIG. 10 is a diagram simply showing another configuration of the seawater flue gas desulfurization apparatus applied to the conventional seawater desulfurization system.
  • another conventional seawater flue gas desulfurization apparatus 107B includes a flue gas desulfurization absorption tower 131 for desulfurizing SO 2 in the exhaust gas 103 to sulfurous acid (H 2 SO 3 ), and a flue gas desulfurization absorption tower.
  • seawater flue gas desulfurization apparatus 107 ⁇ / b> B a part of the seawater 105 ⁇ / b> A for absorption in the seawater 105 supplied via the seawater supply line 112 in the flue gas desulfurization absorption tower 131 is brought into gas-liquid contact with the exhaust gas 103.
  • SO 2 is absorbed by the absorbing seawater 105A.
  • the sulfur-absorbing seawater 106 ⁇ / b> A that has absorbed the sulfur in the flue gas desulfurization absorption tower 131 is mixed with the dilution seawater 105 ⁇ / b> B supplied to the dilution mixing tank 132 provided in the lower part of the flue gas desulfurization absorption tower 131.
  • the sulfur-absorbing seawater 106B mixed and diluted with the dilution seawater 105B is supplied to the oxidation tank 133 provided on the downstream side of the dilution mixing tank 132, and the air 118 is diffused from the oxidation air blower 117. After being supplied through the oxidized air nozzle 120 to recover the water quality, the water is discharged.
  • the flue gas desulfurization absorption tower 131 is installed on the upper side of the dilution mixing tank 132 which becomes a drainage channel of a condenser (not shown) through which the seawater 105 used for dilution flows.
  • the sulfur-absorbing seawater 106A and the seawater 105B supplied to the dilution and mixing tank 132 may not be sufficiently mixed due to a temperature difference between them. There's a problem.
  • the present invention prevents the SO 2 recovered in seawater from being diffused when oxidizing seawater used for desulfurization, and is a safe and highly reliable seawater flue gas desulfurization apparatus. It is another object of the present invention to provide a method for treating desulfurized seawater.
  • a first invention of the present invention for solving the above-mentioned problems is provided integrally with a flue gas desulfurization absorption tower that purifies sulfur content in exhaust gas by contacting with seawater, and under the flue gas desulfurization absorption tower.
  • the sulfur content absorption seawater generated by bringing the sulfur content in the exhaust gas into contact with the seawater and desulfurizing the seawater is mixed and diluted with seawater fed into the main body.
  • the seawater flue gas desulfurization apparatus has a gas retention part including a first weir whose end is buried in the water surface.
  • the length L1 from the side wall of the flue gas desulfurization absorption tower to the inner wall of the first weir is any one of the following formulas (1) and (2): It exists in the seawater flue gas desulfurization apparatus characterized by satisfy
  • d G1 the opening height from the first weir at the outlet of the gas retention section to the bottom of the dilution mixing tank
  • ⁇ 1 the residence time of seawater in the gas retention section
  • U t (dp) the seawater Is the final rising speed of the bubble group having the bubble diameter dp
  • Cc the SO 2 environmental standard concentration
  • C 0 the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the gas-liquid of the bubble an overall mass transfer coefficient of the SO 2 gas at the interface
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank.
  • the terminal rising speed of a single bubble in the static fluid can be obtained from the following Stokes equation (4).
  • U t g ⁇ dp 2 ⁇ ( ⁇ L ⁇ G ) / 18 ⁇ (4)
  • g the gravitational acceleration
  • dp the bubble diameter
  • mu the viscosity of sea water.
  • the bubble diameter exceeds 1 mm, the bubble shape does not become spherical due to friction with the fluid, and the rising speed of the bubble group differs from the behavior of a single bubble, so it does not exactly match, but the bubble in seawater
  • the diameter is usually about 0.5 to 1.0 mm, rarely exceeding 5.0 mm at most, and the terminal ascending rate in the seawater is 200 to 300 mm / s, with a maximum of 400 mm / s. It is about s.
  • the third invention is the seawater flue gas desulfurization apparatus according to the first invention, wherein a second weir is provided at the bottom of the dilution mixing tank.
  • the length L2 from the side wall of the flue gas desulfurization absorption tower to the inner wall of the second weir is any one of the following formulas (5) and (6): It exists in the seawater flue gas desulfurization apparatus characterized by satisfy
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the overall mass transfer coefficient of SO 2 gas at the gas-liquid interface of the bubbles
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank
  • the d G2 is the height of the liquid surface between the seawater liquid surface and the second weir.
  • the fifth invention is the seawater flue gas desulfurization apparatus according to the first invention, wherein a third weir is provided inside the gas retention part.
  • the length L3 from the outer wall of the third weir to the inner wall of the first weir is any one of the following formulas (8) and (9) and the following formula: (10) It is in the seawater flue gas desulfurization apparatus characterized by satisfy
  • d G1 is the opening height from the first weir at the outlet of the gas retention section to the bottom of the dilution mixing tank
  • ⁇ 3 is the residence time of seawater in the gas retention section
  • U t (dp) is the seawater Is the final rising speed of the bubble group having the bubble diameter dp
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the gas-liquid of the bubble an overall mass transfer coefficient of the SO 2 gas at the interface
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank
  • D is a liquid depth of the sea water dilution mixing unit
  • the seventh invention is characterized in that, in the first invention, the second weir is provided at the bottom of the dilution mixing tank, and the third weir is provided inside the gas retention part. Located in smoke desulfurization equipment.
  • the length L4 from the outer wall of the third weir to the inner wall of the second weir is any one of the following formulas (11) and (12) and the following formula: (13) It is in the seawater flue gas desulfurization apparatus characterized by satisfy
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the overall mass transfer coefficient of SO 2 gas at the gas-liquid interface of the bubbles
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank
  • d G1 is the opening height to the bottom of the dilution mixing tank from the first weir
  • d G2 is a sea liquid surface
  • D G3 is the opening height from the third weir to the bottom of the diluting mixing tank
  • MIN (d G1 , d G2 , d G3 ) is: It is the minimum value of d G1 , d G2 , and d G3 .
  • the third weir communicates the space between the gas retention part and the seawater and the flue gas desulfurization absorption tower. It exists in the seawater flue gas desulfurization apparatus characterized by having.
  • a tenth aspect of the invention is the seawater flue gas desulfurization apparatus according to any one of the first to ninth aspects, wherein the seawater is discharged from a condenser.
  • the sulfur component in seawater mixed with the sulfur-absorbing seawater in the dilution / mixing tank is oxidized downstream of the dilution / mixing tank.
  • a seawater flue gas desulfurization apparatus characterized by having an oxidation tank that decarboxylates and recovers water quality.
  • the twelfth invention uses a boiler, exhaust gas discharged from the boiler as a heat source for generating steam, a steam turbine that drives a generator using the generated steam, and water condensed in the steam turbine.
  • a condenser that collects and circulates, a flue gas denitration device that denitrates exhaust gas discharged from the boiler, a dust collector that removes soot in the exhaust gas, and A seawater flue gas desulfurization apparatus and a chimney for discharging the purified gas desulfurized by the flue gas desulfurization apparatus to the outside.
  • the thirteenth invention is to prevent the SO 2 gas contained in the seawater used for the desulfurization using the seawater flue gas desulfurization apparatus according to any one of the first to eleventh inventions from being diffused to the outside. In the processing method of the desulfurization seawater characterized by these.
  • the flue gas desulfurization absorption tower for purifying sulfur in the exhaust gas by contacting with seawater and the flue gas desulfurization absorption tower are integrally provided below the flue gas desulfurization absorption tower, Gas retention provided with a lid having a certain length extending so as to cover the dilution / mixing tank at a connecting portion with the dilution / mixing tank for mixing the sulfur-absorbing seawater with the seawater fed into the main body And has a first weir suspended from the back side of the lid and embedded in the water surface of the dilution mixing tank, so that the sulfur-absorbing seawater is the flue gas desulfurization.
  • Bubbles containing gas having a high SO 2 concentration in the sulfur-absorbing seawater trapped in the seawater by flowing down from an absorption tower in the gas retention part formed by the lid part and the first weir It is possible to prevent the SO 2 gas from leaking outside by being diffused into the space.
  • FIG. 1 is a schematic diagram showing the configuration of a seawater flue gas desulfurization apparatus according to a first embodiment of the present invention.
  • FIG. 2 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the first embodiment of the present invention.
  • FIG. 3 is a schematic view schematically showing a part of the configuration of a conventional seawater flue gas desulfurization apparatus.
  • FIG. 4 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the second embodiment of the present invention.
  • FIG. 5 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the third embodiment of the present invention.
  • FIG. 1 is a schematic diagram showing the configuration of a seawater flue gas desulfurization apparatus according to a first embodiment of the present invention.
  • FIG. 2 is a schematic view schematically showing a part of the configuration of the seawater flue
  • FIG. 6 is a partially enlarged view of the configuration of the seawater flue gas desulfurization apparatus according to the third embodiment of the present invention.
  • FIG. 7 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the fourth embodiment of the present invention.
  • FIG. 8 is a conceptual diagram showing a seawater desulfurization system.
  • FIG. 9 is a diagram illustrating an example of a flow diagram of a thermal power generation system including a seawater flue gas desulfurization device using conventional seawater.
  • FIG. 10 is a diagram simply showing another configuration of the seawater flue gas desulfurization apparatus applied to the conventional seawater desulfurization system.
  • FIG. 1 is a schematic view showing the configuration of the seawater flue gas desulfurization apparatus according to the first embodiment of the present invention
  • FIG. 2 is a simplified diagram of a part of the configuration of the seawater flue gas desulfurization apparatus shown in FIG. FIG.
  • the first seawater flue gas desulfurization apparatus 10-1 removes the sulfur content in the exhaust gas 11 by bringing it into contact with a portion of the seawater 12 for absorbing seawater 12 ⁇ / b> A.
  • a smoke desulfurization absorption tower 13 is provided integrally with the flue gas desulfurization absorption tower 13, and the sulfur content in the exhaust gas 11 is brought into contact with the absorbing sea water 12A in the flue gas desulfurization absorption tower 13 to desulfurize the sea water.
  • the sulfur-absorbing seawater 14A flowing down in the flue gas desulfurization absorption tower 13 produced by the above-mentioned is provided with the dilution seawater 12B fed into the main body 15 and the dilution mixing tank 16 for mixing and diluting, and the flue gas desulfurization absorption tower A lid 18 extending along the longitudinal direction of the dilution / mixing tank 16 so as to cover the dilution / mixing tank 16 on the lower end side of the side wall 17 of the thirteen;
  • the first end 19a is buried in the sea water surface Those having a gas retaining portion 20A that includes a 19.
  • reference numeral 16 a is the bottom of the dilution / mixing tank 16.
  • the seawater 12 is supplied to the flue gas desulfurization absorption tower 13 and used for purification of the exhaust gas 11 as the absorption seawater 12A, and is supplied to the flue gas desulfurization absorption tower 13 for dilution.
  • the seawater used for the dilution is designated as seawater 12B for dilution.
  • the seawater in which the dilution seawater 12B and the sulfur-absorbing seawater 14A flowing down in the flue-gas desulfurization absorption tower 13 are mixed in the flue gas desulfurization absorption tower 13 is referred to as sulfur-absorption seawater 14B.
  • Absorption seawater 12A used in the flue gas desulfurization absorption tower 13 is a part of the seawater 12 extracted by the pump 24 out of the seawater 12 pumped from the sea 21 to the seawater supply line 23 using the pump 22. Absorption seawater 12A is fed to the flue gas desulfurization absorption tower 13. Moreover, although the seawater 12 uses the seawater pumped directly from the sea 21 by the pump 22, the present invention is not limited to this, and the drainage of the seawater 12 discharged from a condenser (not shown) is used. You may make it use.
  • the exhaust gas 11 and the absorbing seawater 12 ⁇ / b> A are brought into gas-liquid contact to desulfurize the sulfur content in the exhaust gas 11. That is, the exhaust gas 11 and the absorbing seawater 12A are brought into gas-liquid contact in the flue gas desulfurization absorption tower 13 to cause a reaction represented by the following formula, and sulfur contained in the exhaust gas 11 in the form of SO 2 or the like.
  • Sulfur content such as oxide (SO x ) is removed using seawater for absorption 12A.
  • the seawater desulfurization causes H 2 SO 3 generated by gas-liquid contact between the absorption seawater 12A and the exhaust gas 11 to dissociate and release H + into the absorption seawater 12A.
  • a large amount of sulfur is absorbed by the sulfur-absorbing seawater 14 ⁇ / b> A flowing down in 13.
  • the pH of the sulfur-absorbing seawater 14A flowing down in the flue gas desulfurization absorption tower 13 is, for example, about 3.
  • the sulfur-absorbing seawater 14 ⁇ / b> A flows down in the flue gas desulfurization absorption tower 13 and is stored in a dilution and mixing tank 16 that is integrally provided on the lower side of the flue gas desulfurization absorption tower 13.
  • the purified gas 25 desulfurized in the flue gas desulfurization absorption tower 13 is released into the atmosphere through the purified gas discharge passage 26.
  • a part of the seawater 12 from the seawater supply line 23 passes through the dilution seawater supply line 27 as dilution seawater 12B and is fed to the dilution mixing tank 16.
  • the sulfur content absorption seawater 14A which flows down in the flue gas desulfurization absorption tower 13 is mixed with the seawater 12B for dilution, and is diluted.
  • Seawater in which the sulfur-absorbing seawater 14A flowing down in the flue gas desulfurization absorption tower 13 and the dilution seawater 12B are mixed is defined as sulfur-absorbing seawater 14B.
  • FIG. 2 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the present embodiment.
  • the first seawater flue gas desulfurization apparatus 10-1 according to the present embodiment has a dilution mixing tank 16 on the lower end side of the side wall 17 on the downstream side of the dilution mixing tank of the flue gas desulfurization absorption tower 13.
  • a cover 18 extending so as to cover the cover 18 and a first weir 19 suspended from the back surface side of the cover 18 and having an end 19a buried in the seawater surface on the water surface in the dilution / mixing tank 16 were provided. It has a gas retention part 20A.
  • the first weir 19 hangs down from the gas retention part 20A, and the sulfur-absorbing seawater 14B in which the dilution seawater 12B and the sulfur-absorbing seawater 14A flowing down in the flue gas desulfurization absorption tower 13 are mixed.
  • the part is dammed in the flue gas desulfurization absorption tower 13.
  • the sulfur-absorbing seawater 14A flows down from the flue gas desulfurization absorption tower 13
  • the bubbles 28 containing the gas having a high SO 2 concentration in the flue gas desulfurization absorption tower 13 are caught in the sulfur-absorption seawater 14B.
  • the bubbles 28 containing SO 2 gas entrained in the sulfur-absorbing seawater 14B are diffused into the space S1 formed by the lid portion 18 and the first weir 19 of the gas retention portion 20A. For this reason, the SO 2 gas entrained in the sulfur-absorbing seawater 14B can remain in the space S1 formed by the lid portion 18 and the first weir 19 of the gas retention portion 19B.
  • FIG. 3 is a schematic view schematically showing a part of the configuration of the conventional seawater flue gas desulfurization apparatus shown in FIG.
  • the conventional seawater flue gas desulfurization apparatus 107B shown in FIG. 3 extends the downstream side wall plate of the dilution and mixing tank of the flue gas desulfurization absorption tower 131 to the sulfur-absorbing seawater 106B of the dilution and mixing tank 132 as it is. The end is buried. Therefore, the conventional seawater flue gas desulfurization apparatus 107B includes a gas having a high SO 2 concentration entrained in the dilution seawater 105B by entrainment of bubbles by the sulfur-absorbing seawater 106A flowing down in the flue gas desulfurization absorption tower 131. There is a risk that bubbles rise and are diffused out of the flue gas desulfurization absorption tower 131, and SO 2 gas leaks to the outside.
  • a lid portion 18 extending from the lower end side of the side wall 17 of the flue gas desulfurization absorption tower 13 so as to cover the dilution / mixing tank 16 and a back surface side of the lid portion 18 are suspended.
  • the gas retention part 20A provided with the first weir 19 whose end is buried in the water surface in the dilution mixing tank 16 is provided, and the end 19a of the first weir 19 is buried in the water surface in the dilution mixing tank 16 And partially immersed in the sulfur-absorbing seawater 14B in the main body 15.
  • the length L1 from the side wall 17 of the flue gas desulfurization absorption tower 13 to the inner wall 19b of the first weir 19 is either one of the following formulas (1) and (2) and the following formula: (3) is satisfied.
  • d G1 is the opening height from the first weir at the outlet of the gas retention section to the bottom of the dilution mixing tank
  • ⁇ 1 is the residence time of seawater in the gas retention section
  • U t (dp) is the seawater Is the final rising speed of the bubble group having the bubble diameter dp
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the gas-liquid of the bubble an overall mass transfer coefficient of the SO 2 gas at the interface
  • the terminal rising speed U t of a single bubble in the static fluid is obtained from the following Stokes equation (4).
  • U t g ⁇ dp 2 ⁇ ( ⁇ L ⁇ G ) / 18 ⁇ (4)
  • g the gravitational acceleration
  • dp the bubble diameter
  • mu the viscosity of sea water.
  • the bubble diameter exceeds 1 mm, the bubble shape does not become spherical due to friction with the fluid, and the rising speed of the bubble group differs from the behavior of a single bubble, so it does not exactly match, but the bubble in seawater
  • the diameter is usually about 0.5 to 1.0 mm, rarely exceeding 5.0 mm at most, and the terminal group rising speed U t in seawater is 200 to 300 mm / s, which is the maximum. However, it is about 400 mm / s.
  • bubbles 28 containing SO 2 gas entrained in the dilution and mixing tank 16 flow into the oxidation tank 29 together with the sulfur-absorbing seawater 14B, and SO 2 is diffused in the oxidation tank 29 to prevent release of an irritating odor. Can do.
  • the gas generated when the quality of the sulfur-absorbing seawater 14B is recovered in the oxidation tank 29 can be diffused in the oxidation tank 29 so as to satisfy the SO 2 environmental standard concentration.
  • the bubbles 28 containing the high-concentration SO 2 gas entrained in the dilution / mixing tank 16 are diffused in the oxidation tank 29 installed on the downstream side of the dilution / mixing tank 16, and the SO 2 gas leaks to the outside. Can be prevented, and a safe and highly reliable seawater desulfurization absorption apparatus can be provided.
  • the sulfur-absorbing seawater 14B is supplied to an oxidation tank 29 provided on the downstream side of the dilution / mixing tank 16.
  • the dilution mixing tank 16 and the oxidation tank 29 are comprised by one tank integrally, this invention is not limited to this, The dilution mixing tank 16 and the oxidation tank 29 are comprised. As a separate tank, the dilution mixing tank 16 and the oxidation tank 29 may be connected.
  • the oxidation tank 29 is provided integrally on the downstream side of the dilution / mixing tank 16, and oxidizes the sulfur content in the sulfur-absorbing seawater 14B and decarboxylates it to restore the water quality.
  • the oxidation tank 29 is provided with an air supply unit 30.
  • the air supply unit 30 includes an oxidizing air blower 32 that supplies air 31, an air diffuser 33 that supplies the air 31, and an oxidized air nozzle 34 that supplies the air 31 to the sulfur-absorbing seawater 14 ⁇ / b> B in the oxidation tank 29.
  • the sulfur-absorbing seawater 14B is recovered by the oxidation reaction of bisulfite ions (HSO 3 ⁇ ) in the sulfur-absorbing seawater 14 and the decarboxylation reaction of bicarbonate ions (HCO 3 ⁇ ). It becomes the recovery seawater 35.
  • the water quality recovery seawater 35 is discharged to the sea 21 as seawater waste liquid through the seawater discharge line 36.
  • the pH of the water-modified seawater 35 can be raised and the COD can be reduced, and the pH, dissolved oxygen concentration, and COD of the water-quality-recovered seawater 35 can be released to a level at which seawater can be discharged.
  • the flue gas desulfurization absorption tower 13 for purifying the sulfur content in the exhaust gas 11 by contacting with the seawater 12A, the exhaust gas Mixing / diluting with the dilution seawater 12B fed into the main body 15 of the sulfur-absorbing seawater 14A provided integrally with the lower side of the smoke desulfurization absorption tower 13 and desulfurizing the seawater in the flue gas desulfurization absorption tower 13
  • a dilution mixing tank 16 a lid 18 extending so as to cover the dilution mixing tank 16 on the lower end side of the side wall 17 of the flue gas desulfurization absorption tower 13, and a drooping and mixing from the back side of the lid 18 It has a gas retention part 20A provided with a first weir 19 whose end 19a is buried in the water surface in the tank 16.
  • the first weir 19 hangs down from the back side of the lid 18, and its end 19 a is buried in the water surface in the dilution and mixing tank 16, and a part of the sulfur-absorbing seawater 14 B is contained in the flue gas desulfurization absorption tower 13. I try to stop it. Accordingly, when the sulfur-absorbing seawater 14A flows down from the flue gas desulfurization absorption tower 13, the bubbles 28 containing the gas having a high SO 2 concentration entrained in the sulfur-absorbing seawater 14B are removed from the lid portion 18 of the gas retaining portion 20A and the first. It is possible to prevent the SO 2 gas from leaking outside by being diffused into the space S1 formed by the one weir 19.
  • a seawater flue gas desulfurization apparatus that can be prevented from being diffused, preventing SO 2 from leaking to the outside, and preventing an irritating odor from being emitted, can be provided.
  • the seawater flue gas desulfurization apparatus which processes the seawater which used the oxidation tank 29 for seawater desulfurization by the flue gas desulfurization absorption tower 13 was demonstrated, this invention is not limited to this. Absent.
  • the oxidation tank 29 desulfurizes sulfur oxides contained in exhaust gas discharged from, for example, factories in various industries, power plants such as large and medium-sized thermal power plants, large boilers for electric utilities, or general industrial boilers. It can be used for the removal of sulfur content in the sulfur-absorbing seawater 14A produced in the above, and desulfurized seawater.
  • FIG. 4 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the present embodiment.
  • the second seawater flue gas desulfurization apparatus 10-2 is the same as the first seawater flue gas desulfurization apparatus 10- according to the first embodiment shown in FIGS. 1 has a gas retention part 20B in which a second weir 42 is provided at the bottom part 16a of one dilution mixing tank 16.
  • the second weir 42 at the bottom 16a of the dilution mixing tank 16
  • the liquid surface between the liquid surface of the sulfur-absorbing seawater 14B and the end 42a of the second weir 42 The height d G2 is reduced. Therefore, the flow rate of the sulfur-absorbing seawater 14B flowing through the oxidation tank 29 is increased, and the bubbles 28 in the sulfur-absorbing seawater 14B are placed between the liquid surface of the sulfur-absorbing seawater 14B and the end 42a of the second weir 42. Can concentrate. As a result, the bubbles 28 can be diffused into the space S1 formed by the lid 18 and the first weir 19 of the gas retention part 20B.
  • the sulfur-absorbing seawater 14A which is the desulfurized flow down liquid
  • the liquid temperature is high because the sulfur-absorbing seawater 14A is in contact with the exhaust gas 11, and the dilution seawater Since the liquid temperature of 12B is low, it is difficult to mix uniformly by simply merging.
  • the second weir 42 is provided at the bottom 16a of the dilution mixing tank 16, the liquid surface between the liquid surface of the sulfur-absorbing seawater 14B and the end 42a of the second weir 42 is provided.
  • the height d G2 is small, and the flow rate of the sulfur-absorbing seawater 14B flowing through the oxidation tank 29 can be increased. For this reason, mixing with the sulfur content absorption seawater 14A and the seawater 12B for dilution can be accelerated
  • the length L2 in the flow direction of the sulfur-absorbing seawater 14B from the side wall 17 of the flue gas desulfurization absorption tower 13 to the inner wall 42b of the second weir 42 is expressed by the following formula (5), ( 6) and the following expression (7) are satisfied.
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the overall mass transfer coefficient of SO 2 gas at the gas-liquid interface of the bubbles
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank
  • the d G2 is the height of the liquid surface between the seawater liquid surface and the second weir.
  • the bubbles 28 containing SO 2 gas in the sulfur-absorbing seawater 14B are more reliably formed by the gas retention part 20B and the first weir 19. Can be diffused into the space S1 and the SO 2 gas can be diffused. This prevents bubbles 28 containing SO 2 gas entrained in the dilution and mixing tank 16 from flowing into the oxidation tank 29 together with the sulfur-absorbing seawater 14B, so that SO 2 is diffused in the oxidation tank 29 and prevents the emission of irritating odors. Can do.
  • the gas generated when the quality of the sulfur-absorbing seawater 14B is recovered in the oxidation tank 29 can be diffused in the oxidation tank 29 so as to satisfy the SO 2 environmental standard concentration.
  • the sulfur content-absorbing seawater flowing into the oxidation tank 29 is provided by providing the second weir 42 at the bottom 16a of the dilution mixing tank 16.
  • the flow rate of 14B is increased, the bubbles 28 are concentrated on the upper surface of the liquid, and the mixing of the sulfur-absorbing seawater 14A and the diluting seawater 12B is promoted in the dilution mixing tank 16, and the bubbles 28 in the sulfur-absorbing seawater 14B are gasified. It can be diffused in the space S ⁇ b> 1 formed by the lid portion 18 of the staying portion 20 ⁇ / b> B and the first weir 19.
  • a high seawater flue gas desulfurization apparatus can be provided.
  • FIG. 5 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the present embodiment
  • FIG. 6 is a partially enlarged view of the configuration of the seawater flue gas desulfurization apparatus according to the present embodiment. It is.
  • the tower of the flue gas desulfurization absorption tower 13 which is a seawater desulfurization absorption tower a large amount of bubbles is absorbed because the sulfur-absorbing seawater 14A which is a large amount of seawater flowing down falls on the dilution mixing tank 16 which is a dilute seawater channel.
  • the amount of foam generated depends on the quality of seawater and the concentration of SO 2 gas in the exhaust gas 11.
  • the dilution mixing tank inside the flue gas desulfurization absorption tower 13 is used. 16 is covered with foam and may flow out to the outside due to the flow of the sulfur-absorbing seawater 14B.
  • the third seawater flue gas desulfurization apparatus 10-3 has a gas retention part 20C in which a third weir 43 is provided inside the gas retention part 20C.
  • the third weir 43 is suspended from the back surface side of the lid 18, the end 43 a is buried in the water surface in the dilution and mixing tank 16, and the seawater 12 ⁇ / b> C is mixed with the seawater 12 ⁇ / b> B and the sulfur-absorbing seawater 14.
  • This part is dammed in the flue gas desulfurization absorption tower 13 to prevent the outflow of bubbles generated inside the flue gas desulfurization absorption tower 13 which is an absorption tower.
  • the partial flow of the sulfur-absorbing seawater 14B is blocked to dilute.
  • the mixing of the sulfur-absorbing seawater 14 ⁇ / b> A and the dilution seawater 12 ⁇ / b> B is promoted, and in the space S ⁇ b> 2 formed by the lid 18, the first dam 19, and the third dam 43 of the gas retention part 20 ⁇ / b> C.
  • the bubbles 28 can be diffused to prevent the SO 2 gas from leaking outside, and the outflow of bubbles generated inside the flue gas desulfurization absorption tower 13 can be prevented.
  • a vent hole 44 is provided to communicate S2 with the flue gas desulfurization absorption tower 13. Therefore, the SO 2 gas filled in the space S2 formed by the lid 18 of the gas retention part 20B, the first dam 19 and the third dam 43 can be diffused to the flue gas desulfurization absorption tower 13 side. .
  • the height d G3 between the end portion 43 a of the third weir 43 and the bottom surface 16 a of the dilution mixing tank 16 is equal to the end portion 19 a of the first weir 19 and the dilution mixing tank 16.
  • the height is the same as the height d G1 between the bottom surface 16a, the height d G1 is not limited to this and may be different.
  • the length L3 in the flow direction of the seawater 12C from the outer wall 43b of the third weir 43 to the inner wall 41a of the first weir 19 is any of the following formulas (8) and (9).
  • the following equation (10) is satisfied.
  • d G1 is the opening height from the first weir at the outlet of the gas retention section to the bottom of the dilution mixing tank
  • ⁇ 3 is the residence time of seawater in the gas retention section
  • U t (dp) is the seawater Is the final rising speed of the bubble group having the bubble diameter dp
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the gas-liquid of the bubble an overall mass transfer coefficient of the SO 2 gas at the interface
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank
  • D is a liquid depth of the sea water dilution mixing unit
  • the air bubbles 28 containing SO 2 gas in the sulfur-absorbing seawater 14B can be more reliably removed from the lid portion 18 and the first weir 19 of the gas retention portion 20C.
  • the third weir 43 can be diffused into the space S2. This prevents bubbles 28 containing SO 2 gas entrained in the dilution mixing tank 16 from flowing into the oxidation tank 29 together with the sulfur-absorbing seawater 14B, so that SO 2 is diffused in the oxidation tank 29 and is prevented from leaking to the outside. It can prevent giving off odor.
  • the gas generated when the quality of the sulfur-absorbing seawater 14B is recovered in the oxidation tank 29 can be diffused in the oxidation tank 29 so as to satisfy the SO 2 environmental standard concentration.
  • the third weir 43 is provided inside the gas retention part 20C in the flow direction of the sulfur-absorbing seawater 14B, and the dilution mixing tank The height of the liquid level between the bottom 16 a of the 16 and the third weir 43 is reduced.
  • the dilution mixing tank 16 mixing with the sulfur content absorption seawater 14A and the dilution seawater 12B is accelerated
  • the bubbles 28 can be diffused into the space S2 to prevent the SO 2 gas from leaking to the outside, and the outflow of bubbles generated inside the flue gas desulfurization absorption tower 13 can be prevented. For this reason, it is possible to prevent the bubbles 28 entrained in the diluting / mixing tank 16 from flowing into the oxidation tank 29 and leaking SO 2 gas to the outside in the oxidation tank 29, and safe and highly reliable seawater.
  • a flue gas desulfurization apparatus can be provided.
  • FIG. 7 is a schematic view schematically showing a part of the configuration of the seawater flue gas desulfurization apparatus according to the present embodiment. As shown in FIG.
  • the seawater flue gas desulfurization apparatus 10-4 according to the fourth embodiment according to the present embodiment is the first according to the first embodiment according to the present invention shown in FIGS.
  • Seawater flue gas desulfurization apparatus 10-1 a second seawater flue gas desulfurization apparatus 10-2 according to the second embodiment of the present invention shown in FIG. 4, and a third implementation according to the present invention shown in FIG.
  • a third seawater flue gas desulfurization apparatus 10-3 according to the above embodiment.
  • the fourth seawater flue gas desulfurization apparatus 10-4 performs dilution so as to cover the dilution mixing tank 16 on the lower end side of the side wall 17 of the flue gas desulfurization absorption tower 13.
  • a first weir 19 that hangs down from the back side of the lid 18 that extends along the longitudinal direction of the mixing tank 16 and whose end 19 a is buried in the water surface in the dilution mixing tank 16;
  • a second weir 42 on the bottom 16a and a third weir 43 hanging from the back side of the lid 18 inside the lid 18 and having its end 43a buried in the water surface in the dilution mixing tank 16 are provided.
  • the first dam 19 and the third dam 43 hang down from the lid 18 and have a sulfur-absorbing seawater 14B in which the dilution seawater 12B and the sulfur-absorbing seawater 14A are mixed. Is partially dammed in the flue gas desulfurization tank 13.
  • the first weir 19 suspended from the back surface side of the lid portion 18 of the gas retaining portion 20D was provided, the second weir 42 was provided at the bottom portion 16a of the dilution mixing tank 16, and the first weir 19 was suspended from the back surface side of the lid portion 18.
  • the third weir 43 As described above, while promoting the mixing of the sulfur-absorbing seawater 14A and the diluting seawater 12B, the flow rate of the sulfur-absorbing seawater 14B flowing toward the oxidation tank 29 is increased, The bubbles 28 containing SO 2 gas in the sulfur-absorbing seawater 14B in the dilution mixing tank 16 can be diffused into the space S2 formed by the first weir 19 and the third weir 43 of the gas retention part 20D. .
  • the length L4 from the outer wall 43b of the third weir 43 to the inner wall 42b of the second weir 42 is either one of the following formulas (11) and (12) and the following formula ( 13) is satisfied.
  • ⁇ 4 L4 / (U L ⁇ D / MIN (d G1 , d G2 , d G3 )) (13)
  • D is the depth of seawater in the dilution mixing tank
  • ⁇ 4 is the residence time of seawater in the gas residence part
  • U t (dp) is the terminal rising speed of the bubble group having the bubble diameter dp in the seawater.
  • Cc is the SO 2 environmental standard concentration
  • C 0 is the SO 2 concentration at the inlet of the flue gas desulfurization absorption tower
  • Kg is the overall mass transfer coefficient of SO 2 gas at the gas-liquid interface of the bubbles
  • dp is the bubble diameter
  • U L is the outlet flow rate of the bottom of the dilution mixing tank
  • d G1 is the opening height to the bottom of the dilution mixing tank from the first weir
  • d G2 is a sea liquid surface
  • D G3 is the opening height from the third weir to the bottom of the diluting mixing tank
  • MIN (d G1 , d G2 , d G3 ) is: It is the minimum value of d G1 , d G2 , and d G3 .
  • the bubbles 28 containing SO 2 gas entrained in the sulfur-absorbing seawater 14B can be more reliably secured to the first weir 19 of the gas retention part 20D.
  • the third weir 43 can be diffused into the space S2. This prevents bubbles 28 containing SO 2 gas entrained in the dilution and mixing tank 16 from flowing into the oxidation tank 29 together with the sulfur-absorbing seawater 14B, so that SO 2 is not diffused to the outside in the oxidation tank 29 and leaks. It can prevent giving off odor.
  • the gas generated when the quality of the sulfur-absorbing seawater 14B is recovered in the oxidation tank 29 can be diffused in the oxidation tank 29 so as to satisfy the SO 2 environmental standard concentration.
  • the mixing of the sulfur-absorbing seawater 14A and the diluting seawater 12B in the dilution-mixing tank 16 is further promoted, and the sulfur-absorption is absorbed.
  • the bubbles 28 in the seawater 14B can be diffused into the space S2 formed by the first weir 19 and the third weir 43 of the gas retention part 20D.
  • FIG. 8 is a conceptual diagram showing a seawater desulfurization system. Since the configuration of the seawater flue gas desulfurization apparatus is the same as that of the seawater flue gas desulfurization apparatus according to the first to fifth embodiments of the present invention, the description thereof is omitted here.
  • the seawater desulfurization system 50 is discharged from the boiler 53, which is burned by a burner (not shown) using air 52 preheated by an air preheater (AH) 51.
  • the exhaust gas 54 is used as a heat source for generating steam, the steam turbine 57 that drives the generator 56 using the generated steam 55, and the condenser 58 that collects and circulates the water 58 condensed by the steam turbine 57.
  • a flue gas denitration device 60 that denitrates the exhaust gas 54 discharged from the boiler 53
  • a dust collector 61 that removes soot and dust in the exhaust gas 54 discharged from the boiler 53
  • the sulfur content in the exhaust gas 54 is converted into seawater
  • a desulfurization apparatus 64 in which the exhaust gas 54 becomes the chimney 66. for discharging purified gas 65 which is desulfurized outside with flue gas desulfurization absorber tower 71.
  • the air 52 supplied from the outside is supplied to the air preheater 51 by the pushing fan 67 and preheated.
  • Fuel (not shown) and air 52 preheated by the air preheater 51 are supplied to the burner, and the fuel is burned by the boiler 53 to generate steam 55 for driving the steam turbine 57.
  • fuel (not shown) used in the present embodiment is supplied from, for example, an oil tank.
  • the exhaust gas 54 generated by combustion in the boiler 53 is sent to the flue gas denitration device 60. At this time, the exhaust gas 54 exchanges heat with the water 58 discharged from the condenser 59 and is used as a heat source for generating steam 55, and the generated steam 55 drives the generator 56 of the steam turbine 57. Then, the water 58 condensed by the steam turbine 57 is returned to the boiler 53 again and circulated.
  • the exhaust gas 54 discharged from the boiler 53 and guided to the flue gas denitration device 60 is denitrated in the flue gas denitration device 60, exchanges heat with the air 52 by the air preheater 51, and then is sent to the dust collector 61.
  • the dust in the exhaust gas 54 is removed.
  • the exhaust gas 54 that has been dust-removed by the dust collector 61 is supplied to the seawater flue gas desulfurization device 64.
  • the seawater flue gas desulfurization apparatus 64 the seawater flue gas desulfurization apparatus according to the present invention is used.
  • the seawater flue gas desulfurization device 64 is provided with a flue gas desulfurization absorption tower 71 for purifying the sulfur content in the exhaust gas 54 by bringing it into contact with a part of the seawater 62A for absorption of the seawater 62, and under the flue gas desulfurization absorption tower 71
  • the sulfur-absorbing seawater 63A generated by bringing the sulfur content in the exhaust gas 54 into contact with the absorbing seawater 62A and desulfurizing in the flue gas desulfurization absorption tower 71 is fed into the main body 72.
  • a gas retaining portion 77 having a lid portion 75 provided and a first weir 76 which is suspended from the back surface side of the lid portion 75 and whose end portion is buried in the water surface in the dilution and mixing tank 73. It is.
  • an oxidation tank 78 is provided integrally with the dilution mixing tank 73 on the downstream side of the dilution mixing tank 73 to oxidize and decarboxylate the sulfur content in the sulfur-absorbing seawater 63B to restore the water quality.
  • the sulfur-absorbing seawater 63B is seawater in which the dilution seawater 62B and the sulfur-absorbing seawater 62A flowing down in the flue gas desulfurization absorption tower 71 are mixed.
  • the oxidation tank 78 is provided with an oxidation air blower 80 for supplying air 79, a diffuser pipe 81 for supplying the air 79, and an oxidation air nozzle 82 for supplying the air 79 to the seawater 62C in the oxidation tank 78. ing.
  • the exhaust gas 54 is supplied into the flue gas desulfurization absorption tower 71 by the induction fan 83. At this time, the exhaust gas 54 is heat-exchanged with the purified gas 65 desulfurized and discharged by the flue gas desulfurization absorption tower 71 by the heat exchanger 84, and then supplied into the flue gas desulfurization absorption tower 71.
  • seawater desulfurization is performed by using a part of the seawater 62 pumped up from the sea 85 as the sulfur content contained in the exhaust gas 54 as the absorption seawater 62A.
  • the exhaust gas 54 produced by burning fossil fuel contains a sulfur content that is sulfur oxide (SO x ) in the form of SO 2 or the like.
  • SO x sulfur oxide
  • seawater 62A of the flue gas desulfurization absorber tower 71 is supplied via the exhaust 54 and the seawater supply line 86 by gas-liquid contact, to absorb SO 2 in the flue gas 54 to absorption seawater 62A, seawater desulfurization Is going.
  • the seawater 62 pumped up from the sea 85 by the pump 87 is heat-exchanged by the condenser 59, and then a part of the seawater 62A for absorption of the seawater 62 that is the drainage of the condenser 59 is exhausted by the pump 88. It is fed to the absorption tower 71. Further, the purified gas 65 desulfurized by the flue gas desulfurization absorption tower 71 is released from the chimney 66 into the atmosphere.
  • the sulfur-absorbing seawater 63A is collected in a dilution and mixing tank 73 that is integrally provided below the flue gas desulfurization absorption tower 71. Further, a part of the seawater 62 is supplied as dilution seawater 62B to the dilution mixing tank 73 via the dilution seawater supply line 89.
  • the sulfur content-absorbing seawater 63A can be diluted with the dilution seawater 62B, and the pH of the sulfur-content-absorbing seawater 63B can be increased.
  • a lid 75 in which a gas retention part 77 is extended along the longitudinal direction of the dilution / mixing tank 73 so as to cover the dilution / mixing tank 73 on the lower end side of the side wall 74 of the flue gas desulfurization absorption tower 71, and this lid 75 has a gas retention part 77 provided with a first weir 76 that hangs down from the back surface side of 75 and whose end is buried in the water surface in the dilution and mixing tank 73.
  • the bubbles 90 containing the high-concentration SO 2 gas entrained in the bottom 73a of the dilution mixing tank 73 are diffused into the space S11 in the gas retention part 77, and remain in this space S11, and the SO 2 gas. Can be prevented from leaking into the downstream oxidation tank 77.
  • air 79 is supplied from the oxidizing air blower 80 through the diffuser pipe 81 into the oxidizing tank 78 from the oxidizing air nozzle 82 to oxidize the bisulfite ions in the sulfur-absorbing seawater 63B and from the bicarbonate ions. Carbon dioxide is desorbed. As a result, the water content of the sulfur-absorbing seawater 63B is recovered and becomes the water-modified seawater 91.
  • the water-modified seawater 91 that has been subjected to the water quality recovery process in the oxidation tank 78 is discharged into the sea 85 as seawater drainage liquid via the seawater discharge line 92.
  • the sulfur-absorbing seawater 63 generated by the seawater desulfurization in the oxidation tank 77 is recovered in the dilution mixing tank 73 and mixed and diluted with the dilution seawater 62B.
  • bubbles 90 containing high-concentration SO 2 gas generated by the flow of the sulfur-absorbing seawater 63A into the dilution seawater 62B at the bottom of the dilution mixing tank 73 are generated in the downstream open oxidation tank 77. Since it can be diffused and SO 2 can be prevented from leaking to the outside, a safe and highly reliable seawater desulfurization system can be provided.
  • the seawater flue gas desulfurization apparatus is externally used when SO 2 entrained in seawater is oxidized when sulfur-absorbed seawater generated by seawater desulfurization is mixed with seawater for dilution. Since it can be prevented from being diffused, it is suitable for use in a seawater flue gas desulfurization apparatus that adjusts so that seawater used for seawater desulfurization can be released to the ocean.

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Abstract

Le premier équipement (10-1) pour la désulfurisation par de l'eau de mer selon l'invention comprend à la fois une tour (13) de désulfurisation/absorption d'un gaz de combustion pour mettre en contact les substances contenant du soufre contenues dans le gaz de combustion (11) avec l'agent d'absorption à base d'eau de mer (12A) (qui est composé en partie d'eau de mer (12)) et purifier ainsi le gaz de combustion, et un réservoir (16) de dilution/mélange qui est disposé exactement en dessous de la tour (13) de désulfurisation/absorption du gaz de combustion et dans lequel l'eau de mer (14A), contenant les substances contenant du soufre (qui est générée dans la tour (13) de désulfurisation/absorption en mettant en contact les substances contenant du soufre contenues dans le gaz de combustion (11) avec l'agent d'absorption à base d'eau de mer (12A) et en désulfurisant ainsi le gaz de combustion avec l'agent d'absorption à base d'eau de mer (12A)), est mélangée et diluée avec de l'eau de mer de dilution (12B) qui est alimentée à l'intérieur du corps (15). En outre, l'équipement (10-1) comprend également une section de séjour du gaz (20A) équipée d'un couvercle (18) qui est fournie sur le côté de l'extrémité inférieure de la paroi latérale (17) de la tour (13) de désulfurisation/absorption du gaz de combustion dans la direction de la longueur du réservoir de dilution/mélange (16) de sorte que le couvercle (18) s'étende au-dessus du réservoir de dilution/mélange (16), et une première crête (19) qui est suspendue du côté arrière du couvercle (18) de sorte que l'extrémité de la crête (19) soit cachée en dessous de la surface de l'eau dans le réservoir de dilution/mélange (16).
PCT/JP2009/058780 2009-05-11 2009-05-11 Equipement pour la désulfurisation d'un gaz de combustion par de l'eau de mer et procédé de traitement de l'eau de mer utilisée lors de la désulfurisation WO2010131327A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
MYPI2011001306A MY170614A (en) 2009-05-11 2009-05-11 Seawater flue-gas desulfurization apparatus and method of treating desulfurization seawater
PCT/JP2009/058780 WO2010131327A1 (fr) 2009-05-11 2009-05-11 Equipement pour la désulfurisation d'un gaz de combustion par de l'eau de mer et procédé de traitement de l'eau de mer utilisée lors de la désulfurisation
KR1020117007344A KR101269707B1 (ko) 2009-05-11 2009-05-11 해수 배연 탈황 장치 및 탈황 해수의 처리 방법
SA109300664A SA109300664B1 (ar) 2009-05-11 2009-11-09 جهاز نزع الكبريت من غازات ا المداخن بماء البحر

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102343209A (zh) * 2011-09-28 2012-02-08 西安交通大学 应用锅炉排污水的烟气海水脱硫系统
WO2013118683A1 (fr) * 2012-02-06 2013-08-15 三菱重工業株式会社 Système de traitement de désulfuration de l'eau de mer
EP2644252A1 (fr) * 2012-03-29 2013-10-02 Doosan Lentjes GmbH Dispositif de purification de gaz combustible
CN114853250A (zh) * 2022-06-06 2022-08-05 萍乡市新安环保工程有限公司 一种焦化脱硫泡沫及废液干燥设备和使用其干燥焦化脱硫泡沫及废液的方法

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KR20180079756A (ko) * 2017-01-02 2018-07-11 한국전력기술 주식회사 해수담수화 설비의 해수농축수를 이용한 해수탈황설비의 구성 및 처리방법

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CN102343209A (zh) * 2011-09-28 2012-02-08 西安交通大学 应用锅炉排污水的烟气海水脱硫系统
CN102343209B (zh) * 2011-09-28 2013-04-17 西安交通大学 应用锅炉排污水的烟气海水脱硫系统
WO2013118683A1 (fr) * 2012-02-06 2013-08-15 三菱重工業株式会社 Système de traitement de désulfuration de l'eau de mer
EP2644252A1 (fr) * 2012-03-29 2013-10-02 Doosan Lentjes GmbH Dispositif de purification de gaz combustible
WO2013143788A1 (fr) * 2012-03-29 2013-10-03 Doosan Lentjes Gmbh Dispositif de purification de fumées
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CN114853250B (zh) * 2022-06-06 2023-02-07 萍乡市新安环保工程有限公司 一种焦化脱硫泡沫及废液干燥设备和使用其干燥焦化脱硫泡沫及废液的方法

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