CN103282101A - Seawater flue-as desulfurization system, and power generating system - Google Patents
Seawater flue-as desulfurization system, and power generating system Download PDFInfo
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- CN103282101A CN103282101A CN2011800611090A CN201180061109A CN103282101A CN 103282101 A CN103282101 A CN 103282101A CN 2011800611090 A CN2011800611090 A CN 2011800611090A CN 201180061109 A CN201180061109 A CN 201180061109A CN 103282101 A CN103282101 A CN 103282101A
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- Prior art keywords
- seawater
- gas desulfurization
- absorption tower
- flue
- exhaust gas
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Links
- 239000013535 sea water Substances 0.000 title claims abstract description 298
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 171
- 230000023556 desulfurization Effects 0.000 title claims abstract description 161
- 239000007789 gas Substances 0.000 claims abstract description 89
- 238000010521 absorption reaction Methods 0.000 claims abstract description 82
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 67
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000003546 flue gas Substances 0.000 claims abstract description 52
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 239000002912 waste gas Substances 0.000 claims description 76
- 239000005864 Sulphur Substances 0.000 claims description 65
- 239000000203 mixture Substances 0.000 claims description 45
- 238000007254 oxidation reaction Methods 0.000 claims description 34
- 230000003647 oxidation Effects 0.000 claims description 33
- 239000007921 spray Substances 0.000 claims description 18
- 238000010926 purge Methods 0.000 claims description 16
- 230000005611 electricity Effects 0.000 claims description 15
- 239000000428 dust Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 239000000779 smoke Substances 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 239000002817 coal dust Substances 0.000 claims description 3
- 238000010790 dilution Methods 0.000 abstract description 14
- 239000012895 dilution Substances 0.000 abstract description 14
- 238000007865 diluting Methods 0.000 abstract description 4
- 238000002156 mixing Methods 0.000 abstract description 4
- 229910052717 sulfur Inorganic materials 0.000 abstract 2
- 239000011593 sulfur Substances 0.000 abstract 2
- 230000009102 absorption Effects 0.000 description 69
- 238000011084 recovery Methods 0.000 description 13
- 239000000284 extract Substances 0.000 description 10
- 230000003009 desulfurizing effect Effects 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- 238000007599 discharging Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 230000033228 biological regulation Effects 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 4
- 229910052815 sulfur oxide Inorganic materials 0.000 description 4
- 238000005276 aerator Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000009792 diffusion process Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000006698 induction Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- YZCKVEUIGOORGS-UHFFFAOYSA-N Hydrogen atom Chemical compound [H] YZCKVEUIGOORGS-UHFFFAOYSA-N 0.000 description 1
- YZCKVEUIGOORGS-IGMARMGPSA-N Protium Chemical compound [1H] YZCKVEUIGOORGS-IGMARMGPSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- DPSZMPUXFZOWAC-UHFFFAOYSA-N [S].S=O Chemical compound [S].S=O DPSZMPUXFZOWAC-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 230000027455 binding Effects 0.000 description 1
- 238000009739 binding Methods 0.000 description 1
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 description 1
- 239000004327 boric acid Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- -1 ocean temperature Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
Images
Classifications
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved 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
-
- 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
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K9/00—Plants characterised by condensers arranged or modified to co-operate with the engines
- F01K9/003—Plants characterised by condensers arranged or modified to co-operate with the engines condenser cooling circuits
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- 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
-
- 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
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/40—Sorption with wet devices, e.g. scrubbers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
- F23J2900/15041—Means for absorbing SOx using seawater
Abstract
This seawater flue-gas desulfurization system (10) is characterized by having: a flue-gas desulfurization absorption tower (11) for purifying exhaust gas (25) by bringing the exhaust gas (25) into gas-liquid contact with seawater (21a); a dilution mixing tank (12) disposed on the downstream side of the flue-gas desulfurization absorption tower (11) and for diluting and mixing, with seawater (21b), sulfur content absorbed seawater (27) containing sulfur content; a seawater supply line (L12) for supplying seawater (21a) to the flue-gas desulfurization absorption tower (11); and surplus seawater branching pipes (L21, L22) diverging from the seawater supply line (L12) at the interior and/or the exterior of the flue-gas desulfurization absorption tower (11) and for supplying seawater (21a) to the dilution mixing tank (12).
Description
Technical field
The system of flue-gas desulfurization with seawater and the electricity generation system that the present invention relates to adopt seawater that the oxysulfide from the waste gas of the discharges such as industrial combustion equipment of coal burning, burning crude oil and heavy oil combustion etc. is carried out desulfurization.
Background technology
In the generating factory that acts as a fuel with coal or former wet goods, in the burning and gas-exhausting gas of discharging from boiler by fossil fuels such as coal are burnt (below, be referred to as " waste gas "), contain oxysulfide sulphur content such as (SOx).For this reason, waste gas will be desulfurized processing, with the sulfur dioxide (SO that contains in the waste gas
2) wait SOx remove the back emit to atmosphere.As such desulfuration processing method, lime lime-gypsum method, spray drying process and seawater method etc. are arranged.
Power plants etc. are owing to need a large amount of cooling waters so build in the place in the face of the sea mostly.For this reason, handle viewpoint considerations such as needed operating cost from suppressing desulfurization, propose a kind of flue-gas desulfurization with seawater device that seawater is carried out the sea water desulfuration of desulfurization as the absorption liquid that absorbs the oxysulfide in the waste gas that adopted.
The flue-gas desulfurization with seawater device carries out the gas-liquid contact to internal feed seawater and the boiler waste gas of the desulfurizing tower (absorption tower) that vertically is placed to the such barrel shape of cylinder roughly or square shape with seawater as absorption liquid, thus SOx is removed.Seawater (sulphur content absorption seawater) after the desulfurization of using as absorbent in desulfurizing tower is for example at long water route (the Seawater Oxidation Treatment System of opened upper end; SOTS) flow in, diluted with sea water mixing and discharge.Sulphur content absorbs micro air bubble that seawater flows out by the air-breather from the local bottom surface of being located at the water route and by carbon dioxide removal (quick-fried gas) (for example, referring to Patent Document 1～3).
In the flue-gas desulfurization with seawater device, when adopting seawater to carry out desulfurization, be adjusted to according to the desulfurization degree of the waste gas of in desulfurizing tower, supplying with and the waste gas of recently obtaining of the waste gas of discharging to the outside of desulfurizing tower and be setting (for example, about 90%).
The prior art document
Patent documentation
Patent documentation 1: TOHKEMY 2006-055779 communique
Patent documentation 2: TOHKEMY 2009-028570 communique
Patent documentation 3: TOHKEMY 2009-028572 communique
Summary of the invention
Invent problem to be solved
When adopting seawater to carry out desulfurization, there is the sulfate ion (SO that contains in the pH value, the seawater after the desulfurization of basicity based on seawater, ocean temperature, seawater
4 2-) seawater proterties such as concentration and the desulfurization degree of waste gas is become than the high situation of setting (for example, about 90%).
When seawater was supplied with in the desulfurizing tower, the adjustment of the quantity delivered of seawater changed to control by the platform number that pump is turned round, and therefore, was difficult to carry out the inching of the quantity delivered of the seawater supplied with in desulfurizing tower.For this reason, when the desulfurization degree of waste gas is higher than setting, there is the such problem of inching of the desulfurization degree that is difficult to carry out waste gas.
The present invention makes in view of above-mentioned problem, and its problem is, system of flue-gas desulfurization with seawater and the electricity generation system of the adjustment of the desulfurization degree that can easily carry out waste gas is provided.
Be used for solving the means of problem
First invention of the present invention that is used for the above-mentioned problem of solution is a kind of system of flue-gas desulfurization with seawater, it is characterized in that having: the exhaust gas desulfurization absorption tower, and it makes waste gas contact and above-mentioned waste gas is cleaned with the seawater gas-liquid; The diluted mixture groove, the back trip side that it is located at above-mentioned exhaust gas desulfurization absorption tower makes the sulphur content that contains sulphur content absorb seawater and carries out diluted mixture with the seawater that dilutes usefulness; The sea water supply pipeline, it is supplied with above-mentioned seawater to above-mentioned exhaust gas desulfurization absorption tower; Residual seawater branch pipe arrangement, its in the tower on above-mentioned exhaust gas desulfurization absorption tower with tower outside in the either party or two sides place from above-mentioned sea water supply line branches, with tower bottom or the either party in the above-mentioned diluted mixture groove or the two sides supply to above-mentioned exhaust gas desulfurization absorption tower of the part of above-mentioned seawater; Control valve, it is arranged on the above-mentioned residual seawater branch pipe arrangement, is used for residual seawater branch component is regulated.
Second invention provides a kind of system of flue-gas desulfurization with seawater on the basis of first invention, it is characterized in that, the branching portion of above-mentioned residual seawater branch pipe arrangement is arranged on the back trip side of the seawater delivery pump of being located at above-mentioned sea water supply pipeline.
The 3rd invention provides a kind of system of flue-gas desulfurization with seawater on the basis of first or second invention, it is characterized in that, the desulfurization degree that obtains according to the desulfurization degree that calculates in the above-mentioned exhaust gas desulfurization absorption tower, calculate oneself to the spray amount of the seawater of the spray nozzle of the above-mentioned seawater of above-mentioned exhaust gas desulfurization absorption tower internal spraying, and the aperture that is arranged on the control valve in the above-mentioned residual seawater branch pipe arrangement adjusted, thus the spray amount of above-mentioned seawater is regulated.
The basis of the 4th invention arbitrary invention in first to the 3rd invention provides a kind of system of flue-gas desulfurization with seawater, it is characterized in that above-mentioned exhaust gas desulfurization absorption tower, above-mentioned diluted mixture groove and oxidation trough are made of same groove.
The 5th invention is characterized in that having: boiler for a kind of electricity generation system; Steam turbine, it will use as the thermal source that steam produces usefulness from the waste gas that above-mentioned boiler is discharged, and utilizes the steam that produces to drive generator; The system of flue-gas desulfurization with seawater of arbitrary invention in first to fourth invention, above-mentioned electricity generation system also has at least one in condenser, smoke evacuation denitrification apparatus, dust collect plant, heat exchanger and the chimney, this condenser reclaims and makes its circulation to the water that condenses in above-mentioned steam turbine, this smoke evacuation denitrification apparatus carries out from the denitration of the waste gas of above-mentioned boiler discharge, this dust collect plant is removed the coal dust in the above-mentioned waste gas, this heat exchanger comprises: heat regenerator makes above-mentioned waste gas and the thermal medium that circulates in heat exchanger carry out heat exchange; Reheater, the Purge gas that above-mentioned thermal medium and the exhaust gas desulfurization absorption tower of above-mentioned waste gas being cleaned from above-mentioned waste gas is contacted with the seawater gas-liquid are discharged is carried out heat exchange, thereby above-mentioned Purge gas is heated again, and this chimney makes in above-mentioned system of flue-gas desulfurization with seawater the Purge gas after the desulfurization discharge to the outside.
The invention effect
According to the present invention, can easily carry out the adjustment of the desulfurization degree of waste gas.
Description of drawings
Fig. 1 is the concise and to the point figure of the formation of the related system of flue-gas desulfurization with seawater of expression embodiments of the invention 1.
Fig. 2 is the figure of an example of expression method of operation that the desulfurization degree of waste gas is adjusted.
Fig. 3 is the concise and to the point figure of the formation of the related electricity generation system of expression embodiments of the invention 2.
The specific embodiment
Below, limit limit with reference to the accompanying drawings is described in detail the present invention.Need to prove, be not to limit the present invention by following embodiment.In addition, the inscape among the following embodiment comprises key element that the art personnel can expect easily or identical in fact, so-called " within the impartial scope ".And then disclosed inscape also can suitably make up in following embodiment.
Embodiment 1
With reference to the accompanying drawings to describing based on embodiments of the invention 1 related system of flue-gas desulfurization with seawater.Fig. 1 is the concise and to the point figure of the formation of expression system of flue-gas desulfurization with seawater.As shown in Figure 1, the related system of flue-gas desulfurization with seawater 10 of present embodiment has exhaust gas desulfurization absorption tower 11, diluted mixture groove 12 and oxidation trough 13.
Exhaust gas desulfurization absorption tower 11 contacts the tower that waste gas 25 is purified for making waste gas 25 with seawater 21a gas-liquid.In exhaust gas desulfurization absorption tower 11, seawater 21a is the ejection of fluid column shape upward from spray nozzle 26, waste gas 25 is contacted with the seawater 21a gas-liquid of supplying with via sea water supply pipeline L12, thereby carry out the desulfurization of the sulphur content in the waste gas 25.In the present embodiment, spray nozzle 26 is the spray nozzle that is the ejection of fluid column shape upward, but is not limited thereto, also can be for being the nozzle of shower shape spraying downwards.
That is, waste gas 25 is contacted with seawater 21a gas-liquid, produces such reaction shown in the following formula (I), make in waste gas 25 with SO
2The sulphur content such as SOx that contain etc. form are absorbed by seawater 21a, thereby utilize seawater 21a that the sulphur content in the waste gas 25 is removed.
SO
2(G)+H
2O→H
2SO
3(L)→HSO
3 -+H
+
…(I)
Under the effect of this sea water desulfuration, contacted with the gas-liquid of waste gas 25 and the H that produces by seawater 21a
2SO
3Disassociation and hydrogen ion (H
+) in seawater 21a, dissociate, so the pH value descends, absorb at sulphur content and absorb a large amount of sulphur content in the seawater 27.Thus, sulphur content absorbs the sulphur content that seawater 27 contains high concentration.At this moment, absorb the pH value of seawater 27 as sulphur content, for example become about 3～6.And the sulphur content that has absorbed sulphur content in exhaust gas desulfurization absorption tower 11 absorbs the tower bottom that seawater 27 accumulates in exhaust gas desulfurization absorption tower 11.The sulphur content that accumulates in the tower bottom on exhaust gas desulfurization absorption tower 11 absorbs seawater 27 and carries via sulphur content absorption seawater discharge pipe L14 and to diluted mixture groove 12.In diluted mixture groove 12, sulphur content absorption seawater 27 mixes with the seawater 21b that supplies with to diluted mixture groove 12 and is diluted.
In addition, the Purge gas after the desulfurization 29 is emitted in atmosphere via Purge gas drain passageway L15 in exhaust gas desulfurization absorption tower 11.
In addition, be provided with the pipe arrangement L21 of residual seawater branch, L22 or this two side at sea water supply pipeline L12.Pump 24 and branching portion 28A exhaust gas desulfurization absorption tower 11 between and with sea water supply pipeline L12 link of the pipe arrangement L21 of residual seawater branch by sea water supply pipeline L12.In addition, the branching portion 28B of the sea water supply pipeline L12 in the pipe arrangement L22 of residual seawater branch and the exhaust gas desulfurization absorption tower 11 links.The residual seawater 21c that extracts out from the pipe arrangement L21 of residual seawater branch, L22 carries to diluted mixture groove 12.Be provided with control valve V11, V12 at the pipe arrangement L21 of residual seawater branch, L22, be used for the amount of the residual seawater 21c that extracts out from the pipe arrangement L21 of residual seawater branch, L22 is adjusted.
The part of seawater 21a is extracted out as residual seawater 21c from sea water supply pipeline L12 by the pipe arrangement L21 of residual seawater branch, L22, the amount of the seawater 21a of the absorption tower of subtend exhaust gas desulfurization easily 11 supplies is adjusted thus, therefore, can easily carry out the adjustment of the desulfurization degree of the waste gas 25 in the exhaust gas desulfurization absorption tower 11.In addition, the ejection of pump 24 is pressed and is suppressed, so can reduce seawater 21a to exhaust gas desulfurization absorption tower 11 power supplied.And then the residual seawater 21c that extracts out to the pipe arrangement L21 of residual seawater branch, L22 supplies with to diluted mixture groove 12, mixes so absorb seawater 27 with sulphur content, can reduce the SO in the sulphur content absorption seawater 27
2Concentration, therefore, the sulphur content that can reduce in the diluted mixture groove 12 absorbs the SO that contains in the seawater 27
2The situation of dispersing again in the atmosphere.
The desulfurization degree of waste gas 25 is according to the entrance SO in the waste gas of supplying with to exhaust gas desulfurization absorption tower 11 25
2Concentration and outlet SO
2The ratio of concentration (outlet SO
2Concentration/entrance SO
2Concentration) or sulphur content absorb the seawater proterties of seawater 27, adjust by the amount of the residual seawater 21c that extracts out to the pipe arrangement L21 of residual seawater branch, L22.
In the present embodiment, so-called " seawater proterties " refers to that sulphur content absorbs basicity, ocean temperature, pH value, the SO of seawater 27
4Concentration etc.So-called " basicity " is for consuming carbonic acid (H
2CO
3), carbanion (CO
3 2-), bicarbonate ion (HCO
3 -), OH
-, organic acid or weak acid the content of composition of acid such as salt (silicic acid, phosphoric acid, boric acid).When the seawater proterties that absorbs seawater 27 according to sulphur content comes the amount of the residual seawater 21c of the pipe arrangement L21 of subtend residual seawater branch, L22 extraction to adjust, absorb basicity, ocean temperature, pH value, the SO of seawater 27 according to sulphur content
4In the concentration at least more than one adjusted the desulfurization degree of waste gas 25.Wherein, as the seawater proterties, preferably according to basicity (HCO
3 -) adjust.
Be provided with for the entrance SO to waste gas 25 at entrance exhaust gas desulfurization absorption tower 11, waste gas 25 and exit
2Concentration and outlet SO
2The SO that concentration is measured
2Densimeter.In addition, in exhaust gas desulfurization absorption tower 11, be provided with for the ocean temperature, pH value, the SO that sulphur content are absorbed seawater 27
4The thermometer that concentration is measured, pH pH-value determination pH device, SO
4Densimeter.
Fig. 2 is the figure of an example of expression method of operation that the desulfurization degree of waste gas 25 is adjusted.As shown in Figure 2, obtain the desulfurization degree of the waste gas 25 in the exhaust gas desulfurization absorption tower 11 and the seawater proterties (step S11) that sulphur content absorbs seawater 27.Whether the desulfurization degree of judging waste gas 25 is threshold value (for example, setting value+α) above (the step S12) of regulation.At this, in the present embodiment, so-called " threshold value of the regulation of desulfurization degree " refers to that for example exhaust gas desulfurization absorption tower 11 is carried out the setting value (for example, desulfurization degree is 90%) of the required regulation of desulfurization and the value of surplus α (for example, desulfurization degree is several %) sum usually.
(for example, when setting value+α) is above, calculate the required spray amount (step S13) of spraying of seawater 21a according to the seawater proterties of sulphur content absorption seawater 27 and the desulfurization degree of waste gas 25 at the desulfurization degree of waste gas 25 for the threshold value of regulation.Calculate the aperture (step S14) of control valve V11, V12 according to the required spray amount of the spraying of seawater 21a.Adjust the switching degree (step S15) of control valve V11, V12 according to the aperture of the control valve V11, the V12 that calculate.
By adjust the switching degree of control valve V11, V12 according to the aperture of the control valve V11, the V12 that calculate, thus can subtend exhaust gas desulfurization absorption tower the amount of the 11 seawater 21a that supply with adjust, therefore can be easily the spray amount of the seawater 21a that sprays out from spray nozzle 26 be adjusted.Thus, as mentioned above, in exhaust gas desulfurization absorption tower 11, can easily carry out the adjustment of the desulfurization degree of waste gas 25.
In addition, in the present embodiment, the pipe arrangement L21 of residual seawater branch, L22 and diluted mixture groove 12 link, the residual seawater 21c that extracts out from the pipe arrangement L21 of residual seawater branch, L22 carries to diluted mixture groove 12, but the supply destination of the residual seawater 21c after extracting out is not limited to diluted mixture groove 12, both can carry to the tower bottom on exhaust gas desulfurization absorption tower 11, also can directly carry to oxidation trough 13.In addition, the residual seawater 21c after the extraction both can carry to diluted mixture groove 12 this two side of tower bottom with exhaust gas desulfurization absorption tower 11, also can carry to oxidation trough 13 this two side of tower bottom with exhaust gas desulfurization absorption tower 11.And then the residual seawater 21c after the extraction also can carry to the tower bottom on diluted mixture groove 12, oxidation trough 13 and exhaust gas desulfurization absorption tower 11.
Diluted mixture groove 12 for the back trip side of being located at exhaust gas desulfurization absorption tower 11, and the sulphur content that will contain sulphur content absorb the groove that seawater 27 and the seawater 21b of dilution usefulness dilute and mix.In diluted mixture groove 12, make by sulphur content in the waste gas 25 is contacted carry out sea water desulfuration sulphur content that produce, that contain sulphur content to absorb seawater 27 with seawater 21a and mix with seawater 21b and dilute.By sulphur content absorption seawater 27 being mixed with seawater 21b and diluting, make the sulphur content in the diluted mixture groove 12 absorb the pH value rising of diluting seawater 31 thus, can prevent SO
2The diffusion again of gas.In addition, diluted mixture groove 12 can prevent SO
2Diffusion and the situation of leaking to the outside can prevent from emitting the situation of pungent odour thus.
And sulphur content absorbs dilution seawater 31 and carries to the oxidation trough 13 in the downstream of being located at diluted mixture groove 12.Oxidation trough 13 carries out the groove that sulphur content absorbs the aerator (air-breather) 32 of the quality recovery processing of diluting seawater 31 for being located at the downstream of diluted mixture groove 12 and having.
The oxidation that aerator 32 has air supply 33 absorbs the oxidation air nozzle 36 that dilution seawater 31 are supplied with the diffuser 35 of air-blaster 34, conveying air 33 and with air 33 to the sulphur content in the oxidation trough 13.Air outside 33 is sent in oxidation trough 13 with nozzle 36 from oxidation air via diffuser 35 with air-blaster 34 by oxidation, the dissolving of the such oxygen of following formula (II) is taken place.Sulphur content absorbs sulphur content in the dilution seawater 31 and contacts with air 33 and the such sulfurous acid hydrogen radical ion (HSO of following formula (III)～(V) takes place in oxidation trough 13
3 -) oxidation reaction and bicarbonate ion (HCO
3 -) carbon dioxide removal reaction, sulphur content absorbs dilution seawater 31 and is resumed water quality, thereby becomes quality recovery seawater 37.
O
2(G)→O
2(L)…(II)
HSO
3 -+1/2O
2→SO
4 2-+H
+…(III)
HCO
3 -+H
+→CO
2(G)+H
2O…(IV)
CO
3 2-+2H
+→CO
2(G)+H
2O…(V)
Thus, the pH value that can make sulphur content absorb dilution seawater 31 rises and reduction COD, thereby the level that quality recovery seawater 37 can seawater be released with pH value, dissolved oxygen concentration, COD is emitted.In addition, even if in oxidation trough 13, carry out producing gas when sulphur content absorbs the quality recovery that dilutes seawater 31, also can make the gas of this generation to satisfy SO
2The mode of environmental criteria concentration spreads in oxidation trough 13.Quality recovery seawater 37 is released to sea 22 via seawater discharge pipe L31.
Like this, in the related system of flue-gas desulfurization with seawater 10 of present embodiment, according to the entrance SO of 11 waste gas of supplying with 25 to the exhaust gas desulfurization absorption tower
2Concentration and outlet SO
2The basicity that the sulphur content when of concentration absorbs seawater 27 comes the amount of the residual seawater 21c that the pipe arrangement L21 of subtend residual seawater branch, L22 extract out to adjust, and can adjust and easily carries out the adjustment of the desulfurization degree of waste gas 25 spray amount of the seawater 21a that sprays out from spray nozzle 26 thus.In addition, can reduce seawater 21a to exhaust gas desulfurization absorption tower 11 power supplied.And then, mixes by making sulphur content in residual seawater 21c and the diluted mixture groove 12 absorb seawater 27, can reduce the SO in the sulphur content absorption seawater 27 thus
2Concentration.Thus, the oxidation trough 13 mobile sulphur content absorption seawater 27 in the outdoor style of opening of subtend carry out oxidation processes and when carrying out quality recovery, can prevent the SO that absorbs in exhaust gas desulfurization absorption tower 11
2Diffusion in diluted mixture groove 12 and make SO
2The situation that gas leaks to the outside, thus can prevent from emitting the situation of pungent odour.
Thereby the system of flue-gas desulfurization with seawater 10 related according to present embodiment can provide stable desulfurization degree and security and the high flue-gas desulfurization with seawater device of reliability of keeping waste gas 25.
In addition, in the present embodiment, be illustrated for the system of flue-gas desulfurization with seawater that in exhaust gas desulfurization absorption tower 11, carries out for the processing of the seawater 21a of sea water desulfuration, but the invention is not restricted to this.The flue-gas desulfurization with seawater device also can be applied to the oxysulfide that contains in power plant, the waste gas of electrical industry with large-sized boiler or discharges such as industrial boiler, iron-smelter, refinery usually such as the factory from various industry for example, large-scale, medium-sized thermal power plant is carried out among the flue-gas desulfurization with seawater device of sea water desulfuration.
In addition, in the present embodiment, exhaust gas desulfurization absorption tower 11, diluted mixture groove 12 and oxidation trough 13 are respectively the groove that is separated from each other independently, and with exhaust gas desulfurization absorption tower 11, diluted mixture groove 12 and oxidation trough 13 bindings, but present embodiment is not limited thereto, both exhaust gas desulfurization absorption tower 11, diluted mixture groove 12 and oxidation trough 13 can be made of a groove as one, also diluted mixture groove 12 and oxidation trough 13 can be made of a groove as one.
Embodiment 2
Describe for embodiments of the invention 2 related electricity generation systems with reference to the accompanying drawings.In the system of flue-gas desulfurization with seawater that is applied to the related electricity generation system of present embodiment, adopted the related system of flue-gas desulfurization with seawater of embodiment 1.Need to prove, for member similarly to Example 1, be marked with same-sign and omit its explanation.
Fig. 3 is the concise and to the point figure of the formation of the related electricity generation system of expression embodiments of the invention 2.As shown in Figure 3, the related electricity generation system 40 of present embodiment has boiler 41, steam turbine 42, condenser 43, smoke evacuation denitrification apparatus 44, dust collect plant 45 and system of flue-gas desulfurization with seawater 10.Need to prove that in the present embodiment, as mentioned above, so-called " sulphur content absorbs seawater 27 " refers to absorb SO in system of flue-gas desulfurization with seawater 10
2Used seawater in sulphur content.
The waste gas 51 that produces in boiler 41 internal combustion is carried to smoke evacuation denitrification apparatus 44.In addition, waste gas 51 thermal source that produces steam 50 as carrying out heat exchange with the water 52 of discharging from condenser 43 uses.Steam turbine 42 adopts this steam 50 to drive generator 53.Then, 43 pairs of water that condense in steam turbine 42 52 of condenser reclaim, and make it return boiler 41 again and circulate.
The waste gas 51 of discharging from boiler 41 carries out denitration in smoke evacuation denitrification apparatus 44, carry out carrying to dust collect plant 45 after the heat exchange with air 48 in air preheater 47, and the coal dust in the waste gas 51 is removed.Then, in system of flue-gas desulfurization with seawater 10, supplied with by induction type fan 55 by the waste gas 51 after dust collect plant 45 dedustings.At this moment, in heat exchanger 56, waste gas 51 carries out with the Purge gas 29 of also being discharged by system of flue-gas desulfurization with seawater 10 desulfurization supplying with in system of flue-gas desulfurization with seawater 10 after the heat exchange.In addition, waste gas 51 also can be obstructed over-heat-exchanger 56 carry out heat exchange with Purge gas 29 and directly supply with to system of flue-gas desulfurization with seawater 10.
In addition, heat exchanger 56 comprises heat regenerator and reheater, and circulation has thermal medium between above-mentioned heat regenerator and above-mentioned reheater.Above-mentioned heat regenerator is arranged between air preheater 47 and the dust collect plant 45, makes the waste gas 51 of discharging from boiler 41 carry out heat exchange with above-mentioned thermal medium.Above-mentioned reheater is located at the back trip side on exhaust gas desulfurization absorption tower 11, makes the Purge gas 57 of 11 discharges from the exhaust gas desulfurization absorption tower carry out heat exchange with above-mentioned thermal medium, thereby Purge gas 29 is heated again.
System of flue-gas desulfurization with seawater 10 is the related flue-gas desulfurization with seawater devices of the above embodiments 1.That is, system of flue-gas desulfurization with seawater 10 has: exhaust gas desulfurization absorption tower 11; Diluted mixture groove 12; Oxidation trough 13; And the pipe arrangement L21 of residual seawater branch, L22.
In system of flue-gas desulfurization with seawater 10, as mentioned above, adopt the sulphur content that from 21 pairs of waste gas 51 of sea 22 seawater that draw, contains to carry out sea water desulfuration.In addition, seawater 21 is drawn from extra large 22 by pump 23, carries out in condenser 43 after the heat exchange, and the seawater 21a of a part carries via sea water supply pipeline L12 and by pump 24 and to system of flue-gas desulfurization with seawater 10.In addition, remaining seawater 21b carries to the upstream side of diluted mixture groove 12 via sea water supply pipeline L13.Waste gas 51 is contacted with seawater 21a gas-liquid, the sulphur content in the waste gas 51 is absorbed by seawater 21a.The sulphur content that has absorbed sulphur content absorb seawater 27 from exhaust gas desulfurization absorption tower 11 upstream side to diluted mixture groove 12 carry, mix with seawater 21b and diluted.
In addition, the waste gas 51 after the purification becomes Purge gas 29 and discharges to the outside from chimney 57 via Purge gas drain passageway L15 in system of flue-gas desulfurization with seawater 10.
In the present embodiment, in the system of flue-gas desulfurization with seawater 10, be provided with the pipe arrangement L21 of residual seawater branch, L22 at sea water supply pipeline L12.The pipe arrangement L21 of residual seawater branch links with sea water supply pipeline L12 between the pump 24 of sea water supply pipeline L12 and exhaust gas desulfurization absorption tower 11.In addition, the sea water supply pipeline L12 in the pipe arrangement L22 of residual seawater branch and the exhaust gas desulfurization absorption tower 11 links.The residual seawater 21c that extracts out from the pipe arrangement L21 of residual seawater branch, L22 carries to diluted mixture groove 12.By utilizing the pipe arrangement L21 of residual seawater branch, L22 from sea water supply pipeline L12 the part of seawater 21a to be extracted out as residual seawater 21c, the amount of the seawater 21a of subtend exhaust gas desulfurization absorption tower 11 supplies is adjusted thus, thereby carries out the adjustment of the desulfurization degree of the waste gas 51 in the exhaust gas desulfurization absorption tower 11.As mentioned above, the desulfurization degree of waste gas 25 is according to the entrance SO in the waste gas of supplying with to exhaust gas desulfurization absorption tower 11 51
2Concentration and outlet SO
2The ratio of concentration (outlet SO
2Concentration/entrance SO
2Concentration) or sulphur content absorb the basicity of seawater 27, adjust by the amount of the residual seawater 21c that extracts out to the pipe arrangement L21 of residual seawater branch, L22.Thereby, can be easily to utilizing the pipe arrangement L21 of residual seawater branch, L22 to adjust from the amount that sea water supply pipeline L12 extracts the part of seawater 21a out, so the amount of the seawater 21a that the absorption tower of subtend exhaust gas desulfurization easily 11 is supplied with is adjusted.Thus, can easily carry out the adjustment of the desulfurization degree of the waste gas 51 in the exhaust gas desulfurization absorption tower 11.In addition, the ejection of pump 24 is pressed and is suppressed, so can reduce seawater 21a to exhaust gas desulfurization absorption tower 11 power supplied.
In addition, from sea 22 seawater that draw 21 carry out heat exchange condenser 43 after, carry to system of flue-gas desulfurization with seawater 10, come for sea water desulfuration, do not carry out heat exchange by condenser 43 and directly carry to system of flue-gas desulfurization with seawater 10 but can make from sea 22 seawater that draw 21 yet, come for sea water desulfuration.
In diluted mixture groove 12, make sulphur content absorb that seawater 27 mixes with seawater 21b and absorbed dilution seawater 31 by the sulphur content after the dilution carries to oxidation trough 13, dilute seawater 31 in 13 pairs of sulphur content absorptions of oxidation trough and recover water quality, become quality recovery seawater 37.The quality recovery seawater 37 that is obtained by oxidation trough 13 is released to sea 22 via seawater discharge pipe L32 from oxidation trough 13 for the form of the level of can seawater releasing with pH value, dissolved oxygen concentration, COD.
In addition, also can the back trip side of the part of the seawater 21 quality recovery seawater 37 in the oxidation trough 13 via dilution sea water supply pipeline L13 be supplied with from sea water supply pipeline L11.Thus, can dilute quality recovery seawater 37 further.Thus, the pH value of quality recovery seawater 37 is risen, and the pH value of seawater discharge opeing is risen near seawater, satisfy the draining benchmark (the pH value is more than 6.0) of the pH value of seawater discharge opeing, and can reduce COD, thereby quality recovery seawater 37 can be emitted with pH value, COD for the form of the level of can seawater releasing.
Like this, the electricity generation system 40 related according to present embodiment, the adjustment of the desulfurization degree of waste gas 51 can be in exhaust gas desulfurization absorption tower 11, easily carried out, and the inhibition that seawater 21a is realized operating cost to exhaust gas desulfurization absorption tower 11 power supplied can be reduced.In addition, the residual seawater 21c that extracts out to the pipe arrangement L21 of residual seawater branch, L22 supplies with to diluted mixture groove 12, can reduce the SO in the sulphur content absorption seawater 27
2Concentration, therefore, the sulphur content that can reduce in the diluted mixture groove 12 absorbs the SO that contains in the seawater 27
2The situation of dispersing again in the atmosphere.Thereby, stable desulfurization degree and security and the high electricity generation system of reliability of both having kept waste gas 51 can be provided.
In addition, the related flue-gas desulfurization with seawater device 10 of present embodiment can utilize among the removing of sulphur content in carry out the sulphur content absorbent solution that sea water desulfuration produces owing to the oxysulfide that contains in to power plants such as the factory from various industry, large-scale, medium-sized thermal power plant, the electrical industry waste gas with large-sized boiler or discharge such as industrial boiler usually.
Symbol description
10 system of flue-gas desulfurization with seawater
11 exhaust gas desulfurization absorption towers
12 diluted mixture grooves
13 oxidation troughs
21,21a, 21b seawater
The 21c residual seawater
22 seas
23,24 pumps
25,51 waste gas
26 spray nozzles
27 sulphur content absorb seawater
28A, 28B branching portion
29 Purge gas
31 sulphur content absorb the dilution seawater
32 aerators (air-breather)
33 air
34 oxidation air-blasters
35 diffusers
36 oxidation air nozzles
37 quality recovery seawater
40 electricity generation systems
41 boilers
42 steam turbines
43 condensers
44 smoke evacuation denitrification apparatus
45 dust collect plants
46 fuel
47 air preheaters (AH)
48 air
49 forced drainages
50 steams
52 water
53 generators
55 induction type fans
56 heat exchangers
57 chimneys
L11, L12 sea water supply pipeline
L13 dilution sea water supply pipeline
L14 sulphur content absorbs the seawater discharge pipe
L15 Purge gas drain passageway
L21, L22 residual seawater branch pipe arrangement
L31, L32 seawater discharge pipe
Claims (5)
1. system of flue-gas desulfurization with seawater is characterized in that having:
The exhaust gas desulfurization absorption tower, it makes waste gas contact and described waste gas is cleaned with the seawater gas-liquid;
The diluted mixture groove, the back trip side that it is located at described exhaust gas desulfurization absorption tower makes the sulphur content that contains sulphur content absorb seawater and carries out diluted mixture with the seawater that dilutes usefulness;
The sea water supply pipeline, it is supplied with described seawater to described exhaust gas desulfurization absorption tower;
Residual seawater branch pipe arrangement, its in the tower on described exhaust gas desulfurization absorption tower with tower outside in the either party or two sides place from described sea water supply line branches, with tower bottom or the either party in the described diluted mixture groove or the two sides supply to described exhaust gas desulfurization absorption tower of the part of described seawater;
Control valve, it is arranged on the described residual seawater branch pipe arrangement, is used for residual seawater branch component is regulated.
2. system of flue-gas desulfurization with seawater as claimed in claim 1 is characterized in that,
The branching portion of described residual seawater branch pipe arrangement is arranged on the back trip side of the seawater delivery pump of being located at described sea water supply pipeline.
3. system of flue-gas desulfurization with seawater as claimed in claim 1 or 2 is characterized in that,
The desulfurization degree that obtains according to the desulfurization degree that calculates in the described exhaust gas desulfurization absorption tower, calculate oneself to the spray amount of the seawater of the spray nozzle of the described seawater of described exhaust gas desulfurization absorption tower internal spraying, and the aperture that is arranged on the control valve on the described residual seawater branch pipe arrangement adjusted, thus the spray amount of described seawater is regulated.
4. as each described system of flue-gas desulfurization with seawater in the claim 1～3, it is characterized in that,
Described exhaust gas desulfurization absorption tower, described diluted mixture groove and oxidation trough are made of same groove.
5. electricity generation system is characterized in that having:
Boiler;
Steam turbine, it will use as the thermal source that steam produces usefulness from the waste gas that described boiler is discharged, and utilizes the steam that produces to drive generator;
Each described system of flue-gas desulfurization with seawater in the claim 1～4,
Described electricity generation system also has at least one in condenser, smoke evacuation denitrification apparatus, dust collect plant, heat exchanger and the chimney,
This condenser reclaims and makes its circulation to the water that condenses in described steam turbine,
This smoke evacuation denitrification apparatus carries out from the denitration of the waste gas of described boiler discharge,
This dust collect plant is removed the coal dust in the described waste gas,
This heat exchanger comprises: heat regenerator makes described waste gas and the thermal medium that circulates in heat exchanger carry out heat exchange; Reheater, the Purge gas that described thermal medium and the exhaust gas desulfurization absorption tower of described waste gas being cleaned from described waste gas is contacted with the seawater gas-liquid are discharged is carried out heat exchange, thereby described Purge gas is heated again,
This chimney makes in described system of flue-gas desulfurization with seawater the Purge gas after the desulfurization discharge to the outside.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2011042962A JP5773687B2 (en) | 2011-02-28 | 2011-02-28 | Seawater flue gas desulfurization system and power generation system |
| JP2011-042962 | 2011-02-28 | ||
| PCT/JP2011/069148 WO2012117586A1 (en) | 2011-02-28 | 2011-08-25 | Seawater flue-gas desulfurization system, and power generating system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103282101A true CN103282101A (en) | 2013-09-04 |
| CN103282101B CN103282101B (en) | 2015-06-03 |
Family
ID=46757540
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201180061109.0A Expired - Fee Related CN103282101B (en) | 2011-02-28 | 2011-08-25 | Seawater flue-as desulfurization system, and power generating system |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JP5773687B2 (en) |
| CN (1) | CN103282101B (en) |
| CL (1) | CL2013001879A1 (en) |
| TW (1) | TWI482657B (en) |
| WO (1) | WO2012117586A1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106029206A (en) * | 2014-09-02 | 2016-10-12 | 富士电机株式会社 | Exhaust gas treatment device and waste water treatment method for exhaust gas treatment device |
| CN108883391A (en) * | 2016-03-31 | 2018-11-23 | 三菱日立电力系统株式会社 | The filler and seawater desulfurization device of packed column |
| CN108934166A (en) * | 2017-03-28 | 2018-12-04 | 三菱日立电力系统株式会社 | The assemble method to ship of the one-piece type desulfurizer of ship desulfurizer, shell, ship and the one-piece type desulfurizer of shell |
| CN109843714A (en) * | 2017-03-24 | 2019-06-04 | 三菱造船株式会社 | The drainage system of ship desulfurizer |
| CN113198294A (en) * | 2021-05-21 | 2021-08-03 | 华能国际电力股份有限公司大连电厂 | Seawater desulfurization control method and equipment |
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| CN104470621B (en) | 2012-12-19 | 2016-10-19 | 富士电机株式会社 | Emission-control equipment |
| KR101740665B1 (en) | 2013-01-29 | 2017-05-26 | 후지 덴키 가부시키가이샤 | Seawater quantity controller for scrubber, seawater quantity control method for scrubber, alkali quantity controller, and alkali quantity control method |
| JP2014233702A (en) * | 2013-06-04 | 2014-12-15 | 三菱重工業株式会社 | Seawater desulfurization device and seawater desulfurization system |
| JP6302191B2 (en) * | 2013-09-02 | 2018-03-28 | 三菱日立パワーシステムズ株式会社 | Power generation system |
| CN105899281B (en) * | 2014-07-18 | 2018-12-14 | 富士电机株式会社 | The seawater amount control device of washer, the seawater amount control method of washer and alkali number control device |
| CN104162361A (en) * | 2014-07-29 | 2014-11-26 | 江苏南极机械有限责任公司 | Device for absorbing and purifying SO2 in diesel engine tail gas by utilizing seawater and absorption method |
| KR101918663B1 (en) | 2018-04-18 | 2018-11-14 | 주식회사 지스코 | Power generation system |
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| CN101557868A (en) * | 2007-02-28 | 2009-10-14 | 三菱重工业株式会社 | System of flue-gas desulfurization with seawater |
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| JPH11244646A (en) * | 1998-03-05 | 1999-09-14 | Ishikawajima Harima Heavy Ind Co Ltd | Control of flow rate of absorbent slurry of stack gas desulfurizer and device therefor |
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| CN102112210B (en) * | 2008-06-13 | 2014-03-26 | 武汉晶源环境工程有限公司 | Method and device for desulfurization of smoke discharged from ship |
| JP5231957B2 (en) * | 2008-11-27 | 2013-07-10 | バブコック日立株式会社 | Wet desulfurization equipment |
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- 2011-02-28 JP JP2011042962A patent/JP5773687B2/en not_active Expired - Fee Related
- 2011-08-25 CN CN201180061109.0A patent/CN103282101B/en not_active Expired - Fee Related
- 2011-08-25 WO PCT/JP2011/069148 patent/WO2012117586A1/en active Application Filing
- 2011-11-28 TW TW100143573A patent/TWI482657B/en not_active IP Right Cessation
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2013
- 2013-06-25 CL CL2013001879A patent/CL2013001879A1/en unknown
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| CN101557868A (en) * | 2007-02-28 | 2009-10-14 | 三菱重工业株式会社 | System of flue-gas desulfurization with seawater |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106029206A (en) * | 2014-09-02 | 2016-10-12 | 富士电机株式会社 | Exhaust gas treatment device and waste water treatment method for exhaust gas treatment device |
| US9821268B2 (en) | 2014-09-02 | 2017-11-21 | Fuji Electric Co., Ltd. | Exhaust gas treatment device and waste water treatment method for exhaust gas treatment device |
| CN108883391A (en) * | 2016-03-31 | 2018-11-23 | 三菱日立电力系统株式会社 | The filler and seawater desulfurization device of packed column |
| CN108883391B (en) * | 2016-03-31 | 2020-12-25 | 三菱动力株式会社 | Filler for packed tower and seawater desulfurization device |
| CN109843714A (en) * | 2017-03-24 | 2019-06-04 | 三菱造船株式会社 | The drainage system of ship desulfurizer |
| CN109843714B (en) * | 2017-03-24 | 2021-09-24 | 三菱造船株式会社 | Drainage system of desulfurization device for ship |
| CN108934166A (en) * | 2017-03-28 | 2018-12-04 | 三菱日立电力系统株式会社 | The assemble method to ship of the one-piece type desulfurizer of ship desulfurizer, shell, ship and the one-piece type desulfurizer of shell |
| CN113198294A (en) * | 2021-05-21 | 2021-08-03 | 华能国际电力股份有限公司大连电厂 | Seawater desulfurization control method and equipment |
Also Published As
| Publication number | Publication date |
|---|---|
| CL2013001879A1 (en) | 2013-11-29 |
| JP2012179521A (en) | 2012-09-20 |
| TWI482657B (en) | 2015-05-01 |
| JP5773687B2 (en) | 2015-09-02 |
| WO2012117586A1 (en) | 2012-09-07 |
| CN103282101B (en) | 2015-06-03 |
| TW201238644A (en) | 2012-10-01 |
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