[go: up one dir, main page]

WO2014156984A1 - Appareil de désulfuration de gaz de combustion à eau de mer et son procédé de fonctionnement - Google Patents

Appareil de désulfuration de gaz de combustion à eau de mer et son procédé de fonctionnement Download PDF

Info

Publication number
WO2014156984A1
WO2014156984A1 PCT/JP2014/057824 JP2014057824W WO2014156984A1 WO 2014156984 A1 WO2014156984 A1 WO 2014156984A1 JP 2014057824 W JP2014057824 W JP 2014057824W WO 2014156984 A1 WO2014156984 A1 WO 2014156984A1
Authority
WO
WIPO (PCT)
Prior art keywords
seawater
circulation tank
spray nozzle
dust removal
desulfurization
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2014/057824
Other languages
English (en)
Japanese (ja)
Inventor
下平　和佳子
今田　典幸
成人 大峰
片川　篤
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Power Ltd
Original Assignee
Babcock Hitachi KK
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Babcock Hitachi KK filed Critical Babcock Hitachi KK
Publication of WO2014156984A1 publication Critical patent/WO2014156984A1/fr
Priority to SA515361205A priority Critical patent/SA515361205B1/ar
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • 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
    • B01D53/504—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 device
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/06—Spray cleaning
    • 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
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/04—Regenerating the washing fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/08—Means for controlling the separation process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/10—Means for removing the washing fluid dispersed in the gas or vapours
    • B01D2247/106—Means for removing the washing fluid dispersed in the gas or vapours using a structured demister, e.g. tortuous channels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B01D2252/1035—Sea water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/206—Organic halogen compounds
    • B01D2257/2064—Chlorine
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/206—Organic halogen compounds
    • B01D2257/2066—Fluorine
    • 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
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • 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

Definitions

  • the present invention relates to a flue gas treatment apparatus for removing harmful components such as sulfur oxide, dust, and heavy metals in exhaust gas generated from a combustion apparatus such as a boiler installed in a thermal power plant or factory, and in particular, wet desulfurization.
  • the present invention relates to a seawater flue gas desulfurization apparatus for removing impurities of high hardness from a desulfurization agent slurry used in the apparatus and an operation method thereof.
  • the combustion exhaust gas contains sulfur oxide (mainly SO 2 ). Since SO 2 is strongly acidic, it must be removed by a flue gas desulfurization device before being discharged from the chimney to the atmosphere.
  • FIG. 2 of Patent Document 1 Japanese Patent Application Laid-Open No. 2001-170444 divides an empty tower portion of an absorption tower having an absorption liquid storage section in which an absorption liquid containing limestone is stored at the lower part into upper and lower stages by a collector,
  • the lower stage is configured as a lower absorbent section having a lower spray nozzle that sprays exhaust gas containing limestone circulated and supplied from the absorbent storage section, and
  • the upper stage is an upper absorbent section provided with an upper spray nozzle that sprays seawater. It is disclosed.
  • Part of the used seawater that has come into contact with the exhaust gas in the upper absorption part is collected by the collector and discharged to the outside of the absorption tower, and the used absorption liquid collected in the absorption liquid storage part is replenished with limestone while being replenished in the lower absorption part. Sprayed from the lower spray nozzle and used for purification of exhaust gas.
  • Japanese Patent Application No. 2012-279808 which is a patent application filed on December 21, 2012 by the present applicant, proposes an exhaust gas treatment apparatus using seawater as shown in FIG.
  • a desulfurization spray nozzle 109 for spraying seawater is installed at the upper part of the desulfurization absorption tower 100, and a partition wall 141 is installed at the lower part of the desulfurization absorption tower 100 to form the inlet-side gas flow path 107.
  • a dust removal spray nozzle 108 that sprays seawater in the circulation tank 103 below the absorption tower to absorb and remove sulfur oxides and dust in the exhaust gas is installed in the inlet side gas flow path 107.
  • a spray nozzle 143 for cleaning the dust spray nozzle 108 is installed on the upper stage.
  • a partition wall 141 in the lower part of the desulfurization absorption tower 100 and narrowing the exhaust gas flow path on the inlet side of the absorption tower, the speed of the exhaust gas introduced into the desulfurization absorption tower 100 is increased, so that a smaller amount of seawater is removed from the dust removal spray nozzle 108. It is possible to improve the dust removal efficiency by spraying.
  • a collector 122 is disposed between the desulfurization spray nozzle 109 and the cleaning spray nozzle 143, and a part of the seawater sprayed from the desulfurization spray nozzle 109 is recovered by the collector 122 and discharged to the sea. It is a configuration.
  • Japanese Patent Application No. 2013-58724 which is a patent application filed on March 21, 2013 by the present applicant, proposes an exhaust gas treatment apparatus using seawater as shown in FIG.
  • a desulfurization liquid spray nozzle 109 for spraying seawater is installed in the upper part of the desulfurization absorption tower 100, and a collector 122 and a collection tank 123 for collecting the sprayed seawater are disposed below the desulfurization spray nozzle 109.
  • the desulfurization spray nozzle 109 is provided between the desulfurization spray nozzle 109 and the collector 122 to absorb the sulfur oxide of the exhaust gas, and the desulfurization spray nozzle 109 is disposed between the exhaust gas inlet duct 107 and the collector 122 located below the collection tank 123.
  • a dust removal spray nozzle 108 is provided, and the dust removal spray nozzle 108 is circulated and supplied with seawater stored in a circulation tank 103 below the desulfurization absorption tower 100.
  • the space between the dust removal spray nozzle 108 and the liquid level of the circulation tank 103 is a dust removal portion B that absorbs and removes soot and heavy metals in the exhaust gas.
  • the sprayed seawater that has come into contact with the exhaust gas from the collector 122 is sent into the oxidation tank 114 and is oxidized by the oxidizing air sucked from the atmosphere through the intake pipe L5 by the microbubble generator 115, and the oxidizing air blower 116 is used. Is oxidized and treated by oxygen dissolved from bubbles blown from the air diffuser nozzle 117 and returned to the ocean 12 as seawater.
  • seawater in the circulation tank is circulated and supplied to the dust removal unit B by a circulation pump to the dust removal spray nozzle, and the seawater sprayed by the spray nozzle is circulated and used, so that concentration gradually proceeds by evaporation, partial dissolution of ash, and the like.
  • the fresh water is replenished to the dust removing section B and the operation is performed so as to obtain a constant concentration by the amount extracted to the waste water treatment facility.
  • the concentration of the sea water in the dust removing section B has the following problems.
  • the spray shape sprayed from the spray nozzle becomes poor, the droplet diameter increases, the spray angle decreases, and the droplet velocity decreases. Occurs.
  • the increase in the viscosity of the liquid may cause a decrease in the liquid / gas ratio, a droplet dispersion failure, and a drop velocity, which may reduce the dust removal efficiency.
  • the amount of soot (including heavy metals) that scatters to the absorption section A in the wake increases due to the increase in the liquid viscosity, the concentration of heavy metals that are trapped in the desulfurization seawater and discharged into the ocean increases. Then, heavy metals that have passed through the absorption part A are discharged from the chimney into the atmosphere.
  • the concentration of seawater in the dust removal portion B does not proceed as much as possible.
  • a scale is generated by a circulation tank, a seawater circulation line, a spray nozzle for spraying seawater, and the like.
  • the concentration of seawater does not proceed as much as possible.
  • the seawater in the dust removal part B is diluted with supplementary seawater to prevent concentration. The amount of seawater extracted to the wastewater treatment facility will increase.
  • the wastewater treatment facility is more efficient and more compact by increasing the concentration of the liquid to be treated and reducing the liquid volume.
  • avoiding the concentration of seawater and increasing the extraction amount will increase the burden on the facility, and if the extraction amount cannot be processed, the facility will have to be enlarged, increasing the installation space and increasing the cost. Leads to.
  • this is inconsistent with the request for avoiding concentration of seawater circulating in the dust removing section B of (1) and (2) above.
  • the object of the present invention is to solve the above-mentioned problems of the prior art by reducing the load of wastewater treatment while preventing scale formation in a circulation tank, a seawater circulation line, a seawater spray nozzle, and the like using seawater that is repeatedly circulated. It is to provide a flue gas desulfurization apparatus and its operation method.
  • an inlet for introducing exhaust gas discharged from a combustion apparatus including a boiler, and a circulation tank provided below the inlet so that fresh seawater is replenished in the circulation tank and at the same time in the circulation tank.
  • a dust removal spray nozzle that absorbs and removes dust and heavy metals in the exhaust gas introduced from the inlet by repeatedly supplying seawater is sprayed, and fresh seawater is sprayed above the dust removal spray nozzle in the exhaust gas introduced from the inlet.
  • An absorption tower provided with a desulfurization spray nozzle for absorbing and removing sulfur oxides, a collector for collecting seawater sprayed from the desulfurization spray nozzle between the dust removal spray nozzle and the desulfurization spray nozzle, and seawater in a circulation tank supplied to the dust removal spray nozzle
  • seawater flue gas desulfurization equipment equipped with a wastewater treatment facility that extracts and stores a part of An indicator correlated with the chlorine (Cl) ion concentration in the seawater in the circulation tank supplied to the dust removal spray nozzle is constantly or intermittently monitored, and the chlorine (Cl) ion concentration derived from the monitoring value exceeds 10 wt%.
  • a seawater flue gas desulfurization apparatus provided with means for adjusting the amount of seawater in a circulation tank withdrawn to a wastewater treatment device and the amount of replenished seawater to be newly replenished into the circulation tank so as not to occur.
  • an inlet for introducing exhaust gas discharged from a combustion device including a boiler, a circulation tank provided below the inlet, and replenishing the circulation tank with fresh seawater, and at the same time in the circulation tank.
  • a dust removal spray nozzle that absorbs and removes dust and heavy metals in the exhaust gas introduced from the inlet by repeatedly supplying seawater is sprayed, and fresh seawater is sprayed above the dust removal spray nozzle in the exhaust gas introduced from the inlet.
  • An absorption tower provided with a desulfurization spray nozzle for absorbing and removing sulfur oxides, a collector for collecting seawater sprayed from the desulfurization spray nozzle between the dust removal spray nozzle and the desulfurization spray nozzle, and seawater in a circulation tank supplied to the dust removal spray nozzle
  • a desulfurization spray nozzle for absorbing and removing sulfur oxides
  • a collector for collecting seawater sprayed from the desulfurization spray nozzle between the dust removal spray nozzle and the desulfurization spray nozzle, and seawater in a circulation tank supplied to the dust removal spray nozzle
  • seawater flue gas desulfurization device equipped with a wastewater treatment facility for extracting and storing a part of An indicator correlated with the chlorine (Cl) ion concentration in the seawater in the circulation tank supplied to the dust removal spray nozzle is constantly or intermittently monitored, and the chlorine (Cl) ion concentration derived from the monitoring value exceeds 10 wt%.
  • the invention according to claim 3 is any one of the viscosity, specific gravity, conductivity, Na ion concentration or Ca ion concentration of the seawater as an index correlated with the chlorine (Cl) ion concentration in the seawater in the circulation tank.
  • the invention according to claim 4 includes a circulation pump for repeatedly supplying seawater in the circulation tank to the dust removal spray nozzle, monitors electric power when driving the circulation pump, and correlates with chlorine in seawater ( Cl) Extract the seawater in the circulation tank into the wastewater treatment facility so that the specific gravity of the seawater in the circulation tank, which correlates with the ion concentration, does not exceed the electric power reaching the preset upper limit value (eg, 1.1).
  • Cl chlorine in seawater
  • the viscosity of the seawater in the circulation tank is 1.6 cP or less, the specific gravity is 1.1 or less, the conductivity is 17 S / m or less, the Na ion is 60,000 ppm or less, and the Ca ion is 1,600 ppm.
  • the seawater according to claim 3 wherein the seawater in the circulation tank is extracted to a wastewater treatment facility, and the same amount of new seawater as that extracted from the circulation tank is replenished in the circulation tank, as corresponding to the following. This is an operation method of the flue gas desulfurization apparatus.
  • an inlet for introducing exhaust gas discharged from a combustion apparatus including a boiler, and a circulation tank provided below the inlet so that fresh seawater is replenished in the circulation tank and at the same time in the circulation tank.
  • a dust removal spray nozzle that absorbs and removes dust and heavy metals in the exhaust gas introduced from the inlet by repeatedly supplying seawater is sprayed, and fresh seawater is sprayed above the dust removal spray nozzle in the exhaust gas introduced from the inlet.
  • An absorption tower provided with a desulfurization spray nozzle for absorbing and removing sulfur oxides, a collector for collecting seawater sprayed from the desulfurization spray nozzle between the dust removal spray nozzle and the desulfurization spray nozzle, and seawater in a circulation tank supplied to the dust removal spray nozzle
  • seawater flue gas desulfurization equipment equipped with a wastewater treatment facility that extracts and stores a part of An indicator correlated with the chlorine (Cl) ion concentration in the treated water discharged from the wastewater treatment facility is constantly or intermittently monitored, and the chlorine (Cl) ion concentration derived from the monitoring value does not exceed 10 wt%.
  • the seawater flue gas desulfurization apparatus is provided with means for adjusting the amount of seawater extracted from the circulation tank to the wastewater treatment apparatus and the amount of replenished seawater newly supplied into the circulation tank.
  • an inlet for introducing exhaust gas discharged from a combustion apparatus including a boiler, a circulation tank provided below the inlet, and replenishing the circulation tank with fresh seawater, and at the same time in the circulation tank.
  • a dust removal spray nozzle that absorbs and removes dust and heavy metals in the exhaust gas introduced from the inlet by repeatedly supplying seawater is sprayed, and fresh seawater is sprayed above the dust removal spray nozzle in the exhaust gas introduced from the inlet.
  • An absorption tower provided with a desulfurization spray nozzle for absorbing and removing sulfur oxides, a collector for collecting seawater sprayed from the desulfurization spray nozzle between the dust removal spray nozzle and the desulfurization spray nozzle, and seawater in a circulation tank supplied to the dust removal spray nozzle
  • a seawater flue gas desulfurization device equipped with a wastewater treatment facility for extracting and storing a part of An indicator correlated with the chlorine (Cl) ion concentration in the treated water discharged from the wastewater treatment facility is constantly or intermittently monitored, and the chlorine (Cl) ion concentration derived from the monitoring value does not exceed 10 wt%.
  • the seawater flue gas desulfurization apparatus operating method is characterized in that the amount of seawater withdrawn from the circulation tank to the wastewater treatment device and the amount of replenishment seawater newly supplied into the circulation tank are adjusted.
  • the invention according to claim 8 measures the concentration of any one or more of chlorine (Cl) ion concentration, Na ion concentration, and Ca ion concentration for the treated water of the waste water treatment facility, and the concentration does not exceed a predetermined value.
  • the circulation tank is configured so that chlorine (Cl) ions are 100,000 ppm or less, Na ions are 60,000 ppm or less, and Ca ions are 1,600 ppm or less.
  • the amount of liquid to be discharged to the wastewater treatment device and the amount of supplementary seawater may be adjusted based on the power of the circulation pump that correlates with the specific gravity of the seawater corresponding to the Cl ion concentration in the seawater of the dust removal unit.
  • the salinity of the seawater repeatedly sprayed and concentrated in the dust removal unit is as high as possible within a range that does not exceed saturation and does not excessively increase the specific gravity and viscosity. Can be maintained.
  • the pressure of the dust removal spray nozzle is lowered, the shape of the sprayed seawater from the dust removal spray nozzle is deteriorated, the spray droplet particle size is increased, the spray angle is decreased, and the dust removal rate in the exhaust gas is decreased due to the decrease of the spray droplet velocity. It is possible to prevent and reduce ash and heavy metals in the exhaust gas after desulfurization.
  • the efficiency of wastewater treatment can be improved, and the facility can be made compact and low in cost.
  • any one or more of the viscosity, specific gravity, conductivity, Na ion concentration or Ca ion concentration of the seawater in the circulation tank is used.
  • the chlorine (Cl) ion concentration of the seawater in the circulation tank can be estimated, and the control becomes easy.
  • the chlorine (Cl) ion concentration in the seawater can be estimated by the electric power when driving the circulation pump, so that the control is easy. It becomes.
  • the viscosity of seawater is 1.6 cP or less, the specific gravity is 1.1 or less, the conductivity is 17 S / m or less, the Na ion is 60,
  • any one or more of the Cl ion concentration, Na ion concentration and Ca ion concentration of the treated water of the waste water treatment facility is measured. Then, the control can be easily performed by adjusting the amount of seawater extracted from the circulation tank to the wastewater treatment device and the amount of replenishment seawater newly supplied into the circulation tank so that the concentration does not exceed a predetermined value.
  • the Cl ion of the treated water of the waste water treatment facility is 100,000 ppm or less, the Na ion is 60,000 ppm or less, the Ca ion is 1, Control can be easily performed by adjusting the amount of seawater extracted from the circulation tank to the wastewater treatment device and the amount of replenishment seawater newly supplied into the circulation tank so as to have a value of 600 ppm or less.
  • FIG. 1 is an overall configuration diagram of an exhaust gas treatment apparatus described in Japanese Patent Application No. 2012-279808 (patent application dated December 21, 2012).
  • 1 is a configuration diagram of an exhaust gas treatment apparatus described in Japanese Patent Application No. 2013-58724 (patent application dated March 21, 2013).
  • FIG. 1 the system
  • the seawater desulfurization apparatus of this embodiment is mainly composed of a desulfurization absorption tower 1 for treating SOx in combustion exhaust gas from a boiler, an inlet duct 2 for introducing exhaust gas into the desulfurization absorption tower 1, and an outlet for exhausting exhaust gas from the desulfurization absorption tower 1.
  • Duct 3 desulfurization spray nozzle 9 that sprays seawater that absorbs sulfur oxide (SOx) in exhaust gas onto exhaust gas, mist eliminator 7 that removes mist accompanying the exhaust gas flow, seawater pump for supplying seawater to desulfurization spray nozzle 9 13.
  • Oxidation tank 14 for oxidizing sulfite ions generated by absorption of SOx
  • oxidation air blower 16 for sending air to be supplied to the oxidation tank 14, air sent from the oxidation air blower 16 via the air supply pipe L6 It is comprised from the aeration nozzle 17 etc. which ejects.
  • Combustion exhaust gas is introduced from the inlet duct 2 into the desulfurization absorption tower 1 in a substantially horizontal direction and discharged from an outlet duct 3 provided at the top of the desulfurization absorption tower 1.
  • the desulfurization absorption tower 1 it is pumped up from the ocean 12 (may be a tank in which seawater is stored) by the seawater pump 13, and sent to the desulfurization spray nozzle 9 as new seawater through the absorption seawater water pipe L1, and the seawater water pipe L3.
  • condensate recovered from a boiler condenser may be supplied in addition to new seawater sent through the absorption seawater water pipe L1.
  • the new seawater sent to the desulfurization spray nozzle 9 is sprayed in the desulfurization absorption tower 1 as fine droplets, and the seawater and the exhaust gas are brought into gas-liquid contact, so that the dust, HCl, HF, etc.
  • SOx mainly SO 2
  • SOx in the exhaust gas is selectively absorbed and removed on the surface of the absorbing droplets of the desulfurization spray nozzle 9.
  • the seawater sprayed from the desulfurization spray nozzle 9 absorbs SOx in the exhaust gas, and the seawater that has absorbed the SOx is rectified by the rectifying member 22 and collected by the collector 10.
  • the inside of the absorption tower 1 between the desulfurization spray nozzle 9 and the collector 10 is referred to as an absorption portion A.
  • the mist accompanying the flow of the exhaust gas is collected by a first mist eliminator 7 installed in the outlet duct 3 at the top of the desulfurization absorption tower 1.
  • the exhaust gas that has passed through the first mist eliminator 7 is reheated as necessary, and then discharged from the chimney 27 into the atmosphere.
  • the booster pump 28 may be used to discharge the purified exhaust gas from the chimney 27.
  • the flow area of the seawater is limited. It is important to arrange the liquid receiving area of the collector 10 below the limited seawater flowing area, and thus all the seawater flowing from the rectifying member 22 can be collected by the collector 10.
  • a dust removal spray nozzle 8 different from the desulfurization spray nozzle 9 is provided in the dust removal portion B which is a region between the collector 10 for collecting the sprayed seawater and the absorbing liquid level composed of the seawater in the circulation tank 5.
  • Absorbing liquid made of seawater stored in a circulation tank 5 below the desulfurization absorption tower 1 is circulated and supplied to the dust removal spray nozzle 8 through the dust removal seawater feed pipe L2 by the absorption liquid circulation pump 4.
  • the absorption liquid (seawater) in the circulation tank 5 is stirred by the stirrer 6 and is oxidized by introduction of oxidized air (not shown).
  • oxidized air not shown.
  • soot and heavy metals in the exhaust gas are absorbed and removed by the absorption liquid composed of dust removal seawater.
  • Part of the absorption liquid consisting of seawater for dust removal in the circulation tank 5 is withdrawn from the seawater pipe L2 for dust removal, and wet treatment for sequentially performing, for example, coagulation sedimentation by adding chemicals ⁇ pH adjustment ⁇ filtration ⁇ neutralization in the wastewater treatment device 24.
  • the solution is purified by a method such as the evaporation method or the evaporation to dryness method, and the treatment liquid is sent to the oxidation tank 14 through the water pipe L5.
  • the treated waste water is not generated.
  • a diffuser nozzle 17 is disposed in the oxidation tank 14, and sulfite is supplied by oxygen dissolved from the bubbles supplied from the oxidizer air blower 16 through the air supply pipe L 6 and ejected from the diffuser nozzle 17. Oxidized and processed and returned to the ocean 12 as seawater.
  • a second mist eliminator 23 is disposed between the dust removal spray nozzle 8 and the collector 10 so that the mist in the seawater sprayed by the dust removal spray nozzle 8 does not reach the absorption part A above the collector 10 and the collector 10. Yes.
  • the desulfurization spray nozzle 9 spreads toward the end.
  • the spread sprayed seawater can flow downward in the vertical direction, and the rectified sprayed seawater can be reliably recovered by the collector 10.
  • the collector 10 uses an upwardly open bowl-shaped member in which two upper and lower stages are arranged in a zigzag manner, and when viewed from above, between the collectors 10 and between the collector 10 at both side ends and the wall surface of the absorption tower 1. Since no gap is generated, new seawater sprayed in a divergent form from the desulfurization spray nozzle 9 of the absorption section A is blocked by the collector 10 and does not flow down to the dust removal section B even if sprayed obliquely downward. .
  • the seawater sprayed from the desulfurization spray nozzle 9 in the absorption section A of the absorption tower 1 is rectified by the rectifying member 22 and flows down while being rectified downward in the vertical direction toward the collector 10, so that the seawater flowing area is limited. For this reason, all the seawater flowing down in the absorption part A can be collected by the collector 10.
  • the seawater sprayed by the absorption part A can fully absorb and remove the sulfur oxide in the exhaust gas by using a large amount of seawater sprayed by the dust removal part B.
  • the seawater stored in the circulation tank 5 can be repeatedly sprayed from the dust removal spray nozzle 8 to absorb and remove the soot and heavy metals in the exhaust gas into the sprayed seawater.
  • the seawater sprayed repeatedly from the dust removal spray nozzle 8 is considerably contaminated with soot and the like as compared with the seawater sprayed by the desulfurization spray nozzle 9 of the absorption section A. After being oxidized in the oxidation tank 14, it is discharged into the ocean 12.
  • a mist eliminator 23 is provided above the dust removal spray nozzle 8 and below the collector 10 to remove the mist.
  • each Example of this invention has disclosed the structure which installed the baffle member 22 and the mist eliminator 23, this invention also includes the case where the baffle member 22 and the mist eliminator 23 are not installed.
  • the specific gravity and viscosity of the seawater circulating in the dust removal part B are used as an index based on the current value (voltage constant) of the power of the circulation pump 4 to the dust removal part B.
  • the replenishment seawater amount is controlled by the control unit 40.
  • This apparatus has the problems (1) and (2) mentioned above.
  • Seawater in the circulation tank 5 circulated and supplied to the dust removal spray nozzle 8 in the dust removal part B evaporates for circulation, and gradually concentrates due to partial dissolution of ash.
  • the viscosity and specific gravity of the liquid increase, the circulation pump 4 is loaded, power increases, the amount of liquid supplied to the dust removal spray nozzle 8 decreases, and the dust removal efficiency may eventually decrease.
  • the current value of the circulation pump 4 is monitored by the ammeter 30, and the control unit 40 extracts the concentrated seawater to the wastewater treatment facility 24 so that the current value corresponding to the specific gravity upper limit of the concentrated seawater is not exceeded.
  • Fresh seawater is supplied to the dust removal section B from the seawater water pipe L7. At this time, by supplying fresh seawater directly into the circulation tank 5, it can be supplied to the dust removal spray nozzle 8 after mixing with the existing concentrated seawater, preventing fluctuations in the spray liquid properties and enabling stable spraying. It becomes.
  • the main component of salinity in seawater is NaCl, and changes in salt concentration when seawater is diluted and concentrated are shown in FIG.
  • Cl 1.6-2 wt%
  • Na 9,000-10,000 ppm.
  • the concentrations of both Cl and Na increase.
  • the Cl concentration is around 20 wt%
  • the dissolved Na ion concentration becomes flat. This indicates that NaCl exceeds the solubility and precipitation occurs.
  • FIG. 3 shows the relationship between dissolved Ca ion concentration and Cl concentration when seawater is diluted and concentrated.
  • Ca is an alkali component
  • the lower the pH the greater the amount of dissolution.
  • the cause of the peak Ca solubility is considered to be the influence of other coexisting ions (Na, SO 4, etc.).
  • the salt concentration in the liquid can also be detected by the conductivity. As shown in FIG. 4, the conductivity of a solution in which NaCl corresponding to a Cl concentration of 10 wt% is dissolved is 17 S / m, so that the conductivity can be controlled to be lower than this.
  • the viscosity is controlled at a specific gravity of 1.1 as the upper limit, and when concentrated to a Cl concentration of 10 wt%, the viscosity is about 1.6 and the influence on the pump power remains small.
  • the specific gravity is about 1.02 when the Cl concentration of the new seawater is about 2 wt% as shown in FIG. 5, but the specific gravity when concentrated to a Cl concentration of 10 wt% is It becomes about 1.1. Further, since the amount of liquid fed by the circulation pump 4 decreases as the specific gravity increases, the amount of sprayed liquid from the dust removal spray nozzle 8 decreases and the liquid / gas ratio decreases.
  • the liquid / gas ratio of the desulfurizer is about 10 to 40 L / m 3 , and within this range, the higher the liquid / gas ratio, the higher the dust removal rate. Directly linked to the decline. Therefore, in order to avoid a large drop in the liquid / gas ratio, it is desirable to control the concentrated seawater with a specific gravity of 1.1 as the upper limit.
  • FIG. 6 shows the relationship between the Cl concentration in the liquid and the viscosity.
  • the viscosity is about 1.2 cP, but the viscosity when concentrated to a Cl concentration of 10 wt% is about 1.6 cP.
  • the circulation seawater in the circulation tank 5 has a specific gravity of about 1.1 and a Cl concentration of 10 wt.
  • the dust removal rate can be controlled to an appropriate value by using a liquid having a viscosity when concentrated to%.
  • FIG. 7 Another embodiment of the present invention is shown in FIG. In the apparatus shown in FIG. 7, members having the same functions as those in the apparatus shown in FIG.
  • the liquid quality of the liquid in the circulation tank 5 or the seawater pipe L2 for dust removal is inspected by the liquid quality monitor 42.
  • the amount of seawater extracted from the circulation tank 5 and the amount of seawater to be supplied to the circulation tank 5 are controlled according to the inspection value.
  • any of the following liquid qualities can be used as an index as a liquid quality correlated with the chlorine (Cl) concentration.
  • Conductivity ⁇ 17S / m electric conductivity meter
  • Liquid viscosity ⁇ 1.6 cP viscosity meter
  • Liquid specific gravity ⁇ 1.1 specific gravity meter
  • Na ion ⁇ 60,000 ppm Na ion meter
  • Ca ion ⁇ 1,600ppm Ca ion meter
  • the liquid in the circulation tank 5 or the seawater pipe L2 for dust removal can be directly measured.
  • specific gravity is batch measurement. Viscosity and conductivity can be measured continuously.
  • the ion meter of Na ion and Ca ion can be continuously measured.
  • the Na measurement upper limit is 230,000 ppm, and there is no problem in the concentration range, but since the pH application range is 4.5 or more, dilution is necessary during measurement.
  • the upper limit of Ca measurement is about 40,000 ppm and the concentration range is not a problem.
  • the pH application range is 5 to 11, dilution is also necessary at the time of measurement.
  • the concentrated seawater of the target dust removal part B is quantitatively extracted into a small (about several liters) dilution tank 43 and diluted. Measurement is performed after quantitatively mixing new seawater (with known ion concentration) in the tank 43. By continuously supplying the concentrated seawater and the new seawater to the dilution tank 43 and discharging them from the dilution tank 43 at the same speed as the total supply speed, continuous measurement is possible.
  • the response membrane of the ion electrode causes a chemical reaction with Hg, so it is directly applied to the concentrated seawater in the dust removal part where Hg in the exhaust gas is dissolved at a high concentration. I can not use it.
  • the amount of seawater withdrawn from the circulation tank 5 and the amount of seawater to be supplied to the circulation tank 5 are controlled so that the proper chlorine ion concentration in the dust removal section B becomes an appropriate value.
  • FIG. 8 Still another embodiment is shown in FIG.
  • the treated water discharged from the waste water treatment facility 24 is extracted from the circulation tank 5 and the amount of seawater supplied to the circulation tank 5 is controlled.
  • One of the following is monitored by the liquid quality monitor 42 as an index of the control, and the controller 40 controls the amount of extracted seawater and the amount of supplementary seawater from the circulation tank 5.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Separation Of Particles Using Liquids (AREA)

Abstract

La présente invention concerne un appareil de désulfuration à eau de mer et son procédé de fonctionnement, l'appareil de désulfuration à eau étant équipé de: une tour d'absorption (1) dotée de buses (8) de pulvérisation de dépoussiérage pour absorber et éliminer la suie et les métaux lourds présents dans les gaz d'échappement et, au-dessus desdites buses (8), des buses (9) de pulvérisation de désulfuration pour absorber et éliminer des SOx dans les gaz d'échappement à l'aide d'eau de mer fraîche, ainsi qu'un collecteur (10) entre les deux sortes de buses (8, 9) pour recueillir l'eau de mer pulvérisée par les buses (9) ; et un appareil de traitement d'effluent (24) pour extraire et recueillir une partie de l'eau de mer dans un réservoir de circulation (5) dans la partie inférieure de la tour d'absorption. Un indice qui est corrélé avec une concentration de Cl- dans l'eau de mer à l'intérieur du réservoir (5) qui est envoyé aux buses (8), est surveillé en continu et de façon intermittente. La formation de tartre sur le réservoir de circulation, les buses de pulvérisation (8,9), etc. est empêchée et la charge de traitement des effluents est réduite en réglant le volume de l'eau de mer dans le réservoir de circulation (5) pour être extrait à l'équipement (24) de traitement des effluents et le volume d'eau de mer rempli pour remplir fraîchement le réservoir de circulation (5) de sorte que la concentration Cl- dérivée de la valeur surveillée ne dépasse pas 10 % en poids.
PCT/JP2014/057824 2013-03-28 2014-03-20 Appareil de désulfuration de gaz de combustion à eau de mer et son procédé de fonctionnement Ceased WO2014156984A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SA515361205A SA515361205B1 (ar) 2013-03-28 2015-09-17 جهاز إزالة الكبريت من غاز متصاعد من تسخين ماء البحر وطريقة تشغيله

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2013-069774 2013-03-28
JP2013069774A JP2014188511A (ja) 2013-03-28 2013-03-28 海水脱硫装置とその運転方法

Publications (1)

Publication Number Publication Date
WO2014156984A1 true WO2014156984A1 (fr) 2014-10-02

Family

ID=51623961

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2014/057824 Ceased WO2014156984A1 (fr) 2013-03-28 2014-03-20 Appareil de désulfuration de gaz de combustion à eau de mer et son procédé de fonctionnement

Country Status (3)

Country Link
JP (1) JP2014188511A (fr)
SA (1) SA515361205B1 (fr)
WO (1) WO2014156984A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108905592A (zh) * 2018-08-17 2018-11-30 中石化南京工程有限公司 一种序批式塔内饱和结晶氨法脱硫装置及方法
CN111439880A (zh) * 2020-04-07 2020-07-24 嘉兴新嘉爱斯热电有限公司 一种零排放的废水处理装置

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NO3085911T3 (fr) * 2015-04-22 2018-05-12
CN104984632A (zh) * 2015-06-25 2015-10-21 莫成杰 一种新型废气污水过滤喷淋塔
JP2018171583A (ja) * 2017-03-31 2018-11-08 三菱日立パワーシステムズ株式会社 無排水化排ガス処理システム及び無排水化排ガス処理方法
CN112194298B (zh) * 2020-08-07 2022-11-01 东方电气集团东方锅炉股份有限公司 一种电厂全厂废水资源化处理系统及方法
CN112535924B (zh) * 2020-11-12 2023-01-03 佛山市南海明涛塑料有限公司 一种热熔尾气处理结构及塑料薄膜回收生产设备
JP7661782B2 (ja) * 2021-05-18 2025-04-15 富士電機株式会社 スクラバ装置
CN115228273B (zh) * 2022-08-12 2023-05-30 中国华电科工集团有限公司 一种海水脱硫系统的控制方法
CN115337731B (zh) * 2022-10-17 2023-04-07 中节能(汕头潮南)环保能源有限公司 一种垃圾焚烧锅炉一体化脱硫负压除尘设备及其除尘方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS61259730A (ja) * 1985-05-13 1986-11-18 Babcock Hitachi Kk 湿式排ガス脱硫装置
JPH07275648A (ja) * 1994-04-07 1995-10-24 Chiyoda Corp 海水利用型湿式排煙脱硫方法および装置
JP2001170444A (ja) * 1999-12-16 2001-06-26 Ishikawajima Harima Heavy Ind Co Ltd 湿式排煙脱硫装置
JP2013039511A (ja) * 2011-08-12 2013-02-28 Babcock Hitachi Kk 湿式排煙脱硫装置およびそれを備えた火力発電プラント

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS61259730A (ja) * 1985-05-13 1986-11-18 Babcock Hitachi Kk 湿式排ガス脱硫装置
JPH07275648A (ja) * 1994-04-07 1995-10-24 Chiyoda Corp 海水利用型湿式排煙脱硫方法および装置
JP2001170444A (ja) * 1999-12-16 2001-06-26 Ishikawajima Harima Heavy Ind Co Ltd 湿式排煙脱硫装置
JP2013039511A (ja) * 2011-08-12 2013-02-28 Babcock Hitachi Kk 湿式排煙脱硫装置およびそれを備えた火力発電プラント

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108905592A (zh) * 2018-08-17 2018-11-30 中石化南京工程有限公司 一种序批式塔内饱和结晶氨法脱硫装置及方法
CN111439880A (zh) * 2020-04-07 2020-07-24 嘉兴新嘉爱斯热电有限公司 一种零排放的废水处理装置

Also Published As

Publication number Publication date
SA515361205B1 (ar) 2016-06-16
JP2014188511A (ja) 2014-10-06

Similar Documents

Publication Publication Date Title
WO2014156984A1 (fr) Appareil de désulfuration de gaz de combustion à eau de mer et son procédé de fonctionnement
JP7390431B2 (ja) 無排水化排ガス処理システム及び無排水化排ガス処理方法
JP2014188406A (ja) 海水排煙脱硫装置とその運用方法
US7964170B2 (en) Method and apparatus for the removal of carbon dioxide from a gas stream
JP3650836B2 (ja) 固体脱硫剤利用湿式排煙脱硫装置と方法
JP5335740B2 (ja) 排ガスの処理方法及び設備
JP6230818B2 (ja) 排ガス処理装置及び排ガス処理方法
JP2015174025A (ja) 海水排煙脱硫装置とその運用方法
JP2013094729A (ja) 排煙脱硫装置
WO2007066443A1 (fr) Appareil et procede humides de desulfuration des gaz de combustion
KR20150010606A (ko) 수은 재방출을 감소시키기 위한 아황산염 제어
US9321006B2 (en) Oxidation control for improved flue gas desulfurization performance
JP2016120438A (ja) 湿式脱硫装置及び湿式脱硫方法
WO2013115108A1 (fr) Cuve d'oxydation, système de désulfurisation des effluents gazeux d'eau de mer et système de génération d'énergie
JP5991664B2 (ja) 排煙脱硫システム
CN104445569A (zh) 用于海水泡沫控制的方法和系统
JP6285773B2 (ja) 排ガス処理装置の排水処理方法
JP5019360B2 (ja) 排煙脱硫装置における過酸化状態発生時の対応方法
JPH10118451A (ja) 排煙処理装置及び排煙処理方法
JP2008178784A (ja) 排煙脱硫装置における亜硫酸カルシウム濃度上昇時の対応方法
JPH11147024A (ja) 排煙処理方法
JP5019361B2 (ja) 排煙脱硫装置における吸収剤スラリ濃度上昇時の対応方法
JP3693778B2 (ja) スラリ中の炭酸塩濃度の制御方法と装置
JP7164344B2 (ja) 酸化還元電位決定装置及びそれを備える脱硫装置、並びに酸化還元電位決定方法
JPH0663353A (ja) 湿式排煙脱硫装置および方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14776402

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: IDP00201506883

Country of ref document: ID

122 Ep: pct application non-entry in european phase

Ref document number: 14776402

Country of ref document: EP

Kind code of ref document: A1