CN110141928A - A kind of device and method of low cost ship wet desulphurization tail gas preparing fresh - Google Patents
A kind of device and method of low cost ship wet desulphurization tail gas preparing fresh Download PDFInfo
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- CN110141928A CN110141928A CN201910409204.3A CN201910409204A CN110141928A CN 110141928 A CN110141928 A CN 110141928A CN 201910409204 A CN201910409204 A CN 201910409204A CN 110141928 A CN110141928 A CN 110141928A
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- 238000000034 method Methods 0.000 title claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000013505 freshwater Substances 0.000 claims abstract description 43
- 238000005507 spraying Methods 0.000 claims abstract description 26
- 238000000746 purification Methods 0.000 claims abstract description 20
- 238000005201 scrubbing Methods 0.000 claims abstract description 20
- 238000001764 infiltration Methods 0.000 claims abstract description 18
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 16
- 238000003860 storage Methods 0.000 claims abstract description 13
- 239000012530 fluid Substances 0.000 claims abstract description 6
- 239000011800 void material Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 72
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 52
- 239000003546 flue gas Substances 0.000 claims description 50
- 239000007788 liquid Substances 0.000 claims description 33
- 239000013535 sea water Substances 0.000 claims description 33
- 239000007921 spray Substances 0.000 claims description 16
- 239000000428 dust Substances 0.000 claims description 15
- 239000002826 coolant Substances 0.000 claims description 11
- 238000001223 reverse osmosis Methods 0.000 claims description 11
- 239000012528 membrane Substances 0.000 claims description 8
- 239000003595 mist Substances 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 4
- 239000000110 cooling liquid Substances 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 3
- 239000008187 granular material Substances 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 4
- 239000010410 layer Substances 0.000 description 70
- 238000009833 condensation Methods 0.000 description 8
- 230000005494 condensation Effects 0.000 description 8
- 230000032258 transport Effects 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 235000019504 cigarettes Nutrition 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 239000003651 drinking water Substances 0.000 description 4
- 235000020188 drinking water Nutrition 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000002356 single layer Substances 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000013618 particulate matter Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
-
- 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
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- 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
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63J—AUXILIARIES ON VESSELS
- B63J1/00—Arrangements of installations for producing fresh water, e.g. by evaporation and condensation of sea water
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- E—FIXED CONSTRUCTIONS
- E03—WATER SUPPLY; SEWERAGE
- E03B—INSTALLATIONS OR METHODS FOR OBTAINING, COLLECTING, OR DISTRIBUTING WATER
- E03B3/00—Methods or installations for obtaining or collecting drinking water or tap water
- E03B3/28—Methods or installations for obtaining or collecting drinking water or tap water from humid air
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/01—Engine exhaust gases
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Biomedical Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- Ocean & Marine Engineering (AREA)
- Public Health (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a kind of device and methods of inexpensive ship wet desulphurization tail gas preparing fresh, and device includes scrubbing tower, buffer tank, counter-infiltration system and fresh water storage tank；Scrubbing tower lower sides or wash tower bottoms are equipped with gas inlet, and top is equipped with exhanst gas outlet, and bottom is equipped with leakage fluid dram in tower；Purification spraying layer, level-one demisting layer, tower body reducer, second level demisting layer, acquisition layer and condensate layer are set gradually in scrubbing tower from the bottom to top；It is cylindrical void tower below tower body reducer, top is square void tower；The outlet of water inlet and acquisition layer at the top of buffer tank, the water outlet of bottom access counter-infiltration system by high-pressure pump；The concentrated water outlet setting control valve of overflow port and counter-infiltration system in the middle part of leakage fluid dram, buffer tank simultaneously accesses outer discharge pipe.Using a large amount of freshwater resources of the recyclable ship wet desulphurization device tail gas of the present invention, fresh water treatment cost is reduced, realizing foreign-going ship, fresh water is self-supporting in the process of running.
Description
Technical field
The present invention relates to resource and environment protection field more particularly to a kind of inexpensive ship wet desulphurization tail gas produce it is light
The device and method of water.
Background technique
In world's cargo transport, transport by sea occupies very big ratio.Ocean-going freight transportation have the traffic capacity it is strong,
Freight volume is big, freight charges are cheap, to the wide adaptability of cargo the features such as.Currently, 2/3rds or more in the total freight volume of international trade,
The 90% of China's cargoes imported and exported transport total amount is all to utilize transport by sea.
Foreign-going ship is longer in the transport by sea duration, and crewman drinks, live and fresh water that equipment on board uses is logical
It crosses bank supply or desalination plant is installed on ship to solve；When feeding fresh water using bank, need to be navigated according to ship
Journey formulates biggish freshwater storage case, occupies the use space of a large amount of foreign-going ship, reduces the carrying capacity of ship；It adopts
Fresh water is made with sea water desalination, not only fresh water cost of manufacture is higher, and device volume is huge, can equally reduce the delivery energy of ship
Therefore power is that current foreign-going ship transports the problem faced if realizing foreign-going ship low cost preparing fresh.
With the sharp increase of ships that transport quantity, foreign-going ship in the process of running, power device exhaust emissions of diesel engine
Pollutant, which is polluted and endangered caused by atmospheric environment and pelagic environment, to be also on the rise.The tail gas of boat diesel engine burning and exhausting
Mainly with sulfur dioxide SO2With nitrogen oxides NO2And based on particulate matter, in order to reduce influence of the ship tail gas to atmospheric environment, closely
Some shipborne equipment manufacturers and scientific research institutions open in terms of ship oxysulfide, Emission Controlling Technology of Nitric Oxides both at home and abroad over year
A large amount of research work is opened up.
It is several more mature to be that developed recently gets up for seawater method, magnesium-based method, calcium base method and sodium base method Wet Flue Gas Desulfurization Technique
Ship tail gas Treatment process, ship tail gas improvement in be most widely used.Ship tail gas wet desulphurization device is using naturally
The desulfurization slurry or desulfuration solution that seawater or seawater and desulfurizing agent are prepared into are reacted with ship high temperature diesel engine vent gas, are neutralized
The pollutants such as the sour gas in flue gas and trap particulate matter are absorbed, to realize the purified treatment of ship tail gas.
It is influenced in ship tail gas wet desulphurization reaction process by gas-liquid temperature difference, high-temperature flue gas steams part evaporation of seawater at water
Gas enters in atmosphere with exhaust emissions.About 30-40 DEG C of ship tail gas delivery temperature for completing wet desulphurization purification, for supersaturation
Flue gas, the water vapour content about 35-40g/Nm in flue gas3, therefore, during transportation, diesel engine vent gas is to ring for foreign-going ship
A large amount of freshwater resources have been discharged in border.If the freshwater resources in tail gas can be recycled, it is high not only to can solve foreign-going ship
Fresh water cost of manufacture, moreover it is possible to the volume of ship fresh water warehouse be greatly reduced, improve the carrying capacity of ship.With a capacity 200,000
Nm3For the middle-size and small-size foreign-going ship of/h, the about 7-8 tons/h of fresh water amount that wet desulphurization tail gas is discharged into environment per hour, if
Therein 30%, which can be recycled, can be realized foreign-going ship fresh water self-sufficiency.
Currently, recycling the technology of freshwater resources from foreign-going ship wet desulphurization tail gas also in blank.
Summary of the invention
The present invention provides a kind of device and methods of inexpensive ship wet desulphurization tail gas preparing fresh, utilize low temperature sea
Water carries out indirect condensing cooling to the saturated flue gas for the wet desulphurization for completing multistage dedusting demisting, the clean liquid in recovered flue gas
Water；Heating that seawater is first exchanged heat is used further to flue gas spray washing, increases the exhaust gas temperature of wet desulphurization saturation tail gas and improves sea
Evaporated quantity of water reduces fresh water cost recovery and improves producing fresh water quantum of output；The fresh water of output is made after reverse osmosis be further processed
For water source of fresh water peculiar to vessel, foreign-going ship fresh water can be greatly reduced using technical solution provided by the invention and produce cost, improve ship
Oceangoing ship fresh water yield improves foreign-going ship voyage.
Specific technical solution is as follows:
A kind of device of low cost ship wet desulphurization tail gas preparing fresh, including scrubbing tower, buffer tank, reverse osmosis system
System and fresh water storage tank；
The scrubbing tower lower sides or wash tower bottoms are equipped with gas inlet, and top is equipped with exhanst gas outlet, bottom in tower
Equipped with leakage fluid dram；Inside scrubbing tower and be located above gas inlet set gradually from the bottom to top purification spraying layer, level-one demisting layer,
Tower body reducer, second level demisting layer, acquisition layer and condensate layer；It is cylindrical void tower below the tower body reducer, top is
Square void tower；
Water inlet is equipped at the top of the buffer tank, middle part is equipped with overflow port, and bottom is equipped with water outlet；The water inlet is logical
The outlet of pipeline and acquisition layer is crossed, the water outlet imports and exports connecting line and counter-infiltration system water inlet by high-pressure pump
Connection；
Concentrated water outlet and the outer discharge pipe of the leakage fluid dram of the scrubbing tower, the overflow port of buffer tank and counter-infiltration system
Connection.
Based on same inventive concept, the present invention also provides a kind of inexpensive ship wet desulphurization tail gas preparing freshs
Method is preferably realized by the device of the inexpensive ship wet desulphurization tail gas preparing fresh, comprising the following steps:
(1) ship tail gas is passed through in scrubbing tower by gas inlet, by seawater as purification spraying layer spray liquid to ship
Vessel exhaust is washed, is cooled down, is humidified, and saturation wet flue gas is obtained；
(2) the saturation wet flue gas enters level-one demisting layer, removes partial particulate dust and saliferous droplet；
(3) after level-one demisting, wet flue gas enters top tower body through tower body reducer, into second level demisting layer, further
Granule dust and saliferous droplet are removed, clean saturation wet flue gas is obtained；
(4) clean saturation wet flue gas passes through acquisition layer and rises to condensate layer, and cooling reaches hypersaturated state in condensate layer,
Water recovery therein is at liquid clean water and falls to acquisition layer, is discharged into buffer tank by acquisition layer outlet；It completes multistage
Flue gas after condensation receipts water is discharged by exhanst gas outlet；
(5) clean water by high-pressure pump be sent into counter-infiltration system, after reverse osmosis membrane concentration obtain fresh water and
Concentrated water.
The fresh water of acquisition is used for drinking water and domestic water, and the concentrated water of acquisition is with the purification spraying layer for completing desulfurization, dedusting
Cleaning solution is discharged into ocean.
The device of the inexpensive ship wet desulphurization tail gas preparing fresh further includes coolant pump；
The purification spraying layer includes upper layer purification spraying layer and lower layer's purification spraying layer；
The water outlet pipeline of the coolant pump is divided into two-way, is connected all the way by the cooling liquid inlet of pipeline and condensate layer
Logical, the cooling liquid outlet of the condensate layer purifies the spray liquid inlet communication of spraying layer by pipeline and lower layer；Another way passes through
The spray liquid inlet communication of pipeline and upper layer purification spraying layer.
In step (1), ship tail gas is entered in scrubbing tower by gas inlet, through two layers seawater spraying desulfurization, dedusting.Lower layer
It purifies spraying layer and is evaporated using the high temperature seawater after condensate layer heat exchange as spray liquid, high temperature seawater and the heat exchange of high-temperature ship tail gas
A large amount of fresh water steam out；Upper layer purification spraying layer directly extracts low temperature seawater and is cooled down to ship tail gas, is humidified, in wet flue gas
Part vapor is condensed by nucleus of dust, is formed liquid water and is fallen to outside scrubbing tower tower reactor discharge tower with spray liquid, while cigarette
The further evaporative condenser of gas simultaneously reaches saturation state.
Here low temperature seawater and high temperature seawater is that in contrast, low temperature seawater refers to the sea directly extracted from ocean
Water, high temperature seawater refer to condensate layer discharge with high-temperature ship tail gas heat exchange after seawater.
Preferably, the demister in the level-one demisting layer be baffle type mist eliminator, the baffle type mist eliminator into
Mouth end exhaust gases passes are greater than middle part and outlet end exhaust gases passes.
Input end exhaust gases passes are big, the biggish seawater atomized drop of removal partial size and dust particle, middle part and outlet end
Exhaust gases passes are small, the lesser atomized drop of removal partial size and dust particle, reduce the risk and demister resistance of demister blocking
Power.
It is further preferred that baffle(s) spacing 5-20mm, the long difference of input end adjacent panels is 10- in level-one demisting layer
150mm, demister height are 0.2-1.0m.
In level-one demisting layer, baffle plate is different in size, and long baffle plate is arranged alternately with short baffle plate, demister input end
The length difference of adjacent baffle is 10-150mm.
Scrubbing tower is divided into two sections, and two sections are docked by tower body reducer.The cigarette of tower body above tower body reducer
Gas flow cross is greater than the flue gas flow cross of lower section tower body.
After flue gas enters top tower body by lower section tower body, flue gas flow rate is reduced, and extends flue gas in second level demisting layer and cold
The residence time of solidifying layer, so as to reduce the demister and condenser height in second level demisting layer.
Preferably, the cross section of tower body is circle below tower body reducer, and the cross section of tower body is above tower body reducer
It is rectangular；The side length of upper section square tower body cross section is 1.0-1.5 times of the diameter of lower section circle tower body cross section.
Demister in the second level demisting layer is that the ridge type demister to be formed is arranged using plate.Ridge type demister
Flue gas area of passage can be increased, reduce flue gas flow rate, help to capture the fine drop that flue gas carries, while removing liquid in flue gas
Drip the soluble-salt carried.
Preferably, the demister in the second level demisting layer is located at 0.5-1.0m above tower body reducer, second level demisting layer
High 0.5-2.0m.
It is further preferred that the plate spacing of the ridge type demister is 5-20mm.
Ship tail gas is washed by two layers of spray heat exchange condensation and two-stage demister dedusting demisting, and pollutant obtains in tail gas
Deep purifying obtains clean saturation wet flue gas, and wherein the liquid water droplets of second level demister trapping fall to level-one demisting layer to one
Grade demister surface is rinsed, and removes the pollutant on level-one demister surface, realizes zero water consume of level-one demister from flushing.
1~4 layer of condenser is set in the condensate layer；The heat exchange element of condenser is made of heat exchanger tube and baffling blade.
Condensate liquid high in and low out in heat exchanger tube.Baffle plate blade, which plays, increases condenser heat exchange area, trapping condensing droplet recycle-water
With the effect of support heat exchanger.
Preferably, every layer of condenser water inlet is individually connected with coolant pump outlet supervisor by pipeline, and sets valve list
The coolant rate of every layer of condenser is solely controlled, so that adjusting flue-gas temperature reduces amplitude, realizes the condensing recovery of control steam
Yield.
Preferably, lower layer's condenser is 0.3-0.8m, single layer away from liquid trap 0.3-1.0m, the spacing of adjacent two layers condenser
Condenser height is 0.3-1.5m.
Preferably, the flue gas cool-down amplitude for controlling single layer condenser is 0.5-5 DEG C.
One water inlet is set at the top of the buffer tank, an overflow port is arranged in middle part, and a water outlet is arranged in bottom,
Control valve and outlet pipeline connection is arranged by the pump inlet of piping connection high pressure, middle part overflow port in bottom water outlet.It is living
In the case that drinking water storage is sufficient, closing reverse osmosis filtration system, the clean water overflow that acquisition layer is collected to buffer tank, and
By overflow port overflow in the middle part of buffer tank to outer discharge pipe, condenser water inlet valve is also adjusted, reduces low temperature seawater flow,
Control cooling capacity.
The water inlet of the counter-infiltration system is connected by pipeline with high pressure pump outlet, the concentrated water water outlet of counter-infiltration system
With outlet pipeline connection, fresh water outlet mouth is connected to fresh water storage tank.Preferably, the reverse osmosis membrane of the counter-infiltration system is using pipe
Formula film；The operating pressure of reverse osmosis membrane is 2-10MPa, is discharged fresh water salt content < 0.05%.
It is low or when fresh water dosage is big in ship power system load, condenser water inlet valve is adjusted, low temperature seawater is increased
Flow improves condensation number and fresh water yield, and counter-infiltration system concentrated water can also be back to buffer tank, and preparing fresh is concentrated.
It is further preferred that the operating pressure of reverse osmosis membrane is 2-10MPa, it is discharged fresh water salt content < 0.05%.
Compared with prior art, the invention has the benefit that
(1) the present invention provides a kind of solution of inexpensive ship tail gas deep purifying, increased using variable diameter and washed
The sectional area of tower (desulfurizing tower) upper section reduces demisting condensation segment flue gas flow rate, extends demisting condensation time, improves gas cleaning effect
Rate；Flue gas flow rate of the flue gas in demister is further decreased using ridge type demister, realizes particulate matter and saliferous drop
Deep purifying improves fresh water water quality and reduces condensate liquid processing cost；
(2) the present invention provides one kind, and low cost can be achieved, high efficiency recycles freshwater resources in ship wet desulphurization tail gas
Solution；It is used for wet desulphurization agent using the high temperature seawater for completing condensing heat-exchange, greatly improves wet-method desulfurized fume
Exhaust gas temperature and evaporation of seawater amount, improve the water yield of condensation process, reduce condensing hot air furnace cost, it can be achieved that foreign-going ship without
Fresh water need to be carried and carry out continuous navigation for a long time.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of apparatus of the present invention；Wherein:
1- scrubbing tower, 2- coolant pump, 3- buffer tank, 4- high-pressure pump, 5- counter-infiltration system, 6- fresh water storage tank, 1-1 cigarette
Gas import, 1-2 spraying layer, 1-3 level-one demister, 1-4 tower body reducer, 1-5 second level demister, 1-6 liquid trap, 1-7 condensation
Layer, 1-8 chimney.
Specific embodiment
As shown in Figure 1, the device that the technique of present invention low cost ship wet desulphurization tail gas preparing fresh is based on includes:
Scrubbing tower 1, coolant pump 2, buffer tank 3, high-pressure pump 4, counter-infiltration system 5, fresh water storage tank 6, wherein scrubbing tower 1 is from the bottom to top
Set gradually washing tower reactor, gas inlet 1-1, spraying layer 1-2, level-one demister 1-3, tower body reducer 1-4, second level demister
1-5, liquid trap 1-6, condensate layer 1-7 and the outlet chimney 1-8.
Ship tail gas enters scrubbing tower 1 by gas inlet 1-1, through two layers of seawater spraying desulfurization in spraying layer 1-2, simultaneously
Lower layer purifies spray liquid using high temperature seawater after heat exchange, evaporates a large amount of fresh water steam, upper layer purification spray with high-temperature flue gas heat exchange
It drenches liquid and decreasing temperature and increasing humidity is carried out to tail gas using low temperature seawater, part vapor is condensed by nucleus of dust in wet flue gas, forms liquid
State water falls to washing tower reactor with the cold liquid of spray and is discharged outside tower, and most of partial size larger particles dust is gone in flue gas
It removes.
After completing spray washing, saturation wet flue gas carries a small amount of fine particle dust and the sea water drops of saliferous enter level-one
Demister 1-3, flue gas pass through the baffle plate demister that channel narrows from the width, large-size particles dust and seawater at fat pipe position
Atomized drop inertia force effect under with baffle plate they strike and be captured, particle dust and drop are relatively narrow in flow area
Locate to collide with baffle plate blade captured, is saturated the pollutants such as dust and saliferous drop in wet flue gas and obtains depth removal.
Complete primary dust removing, the saturation wet flue gas of demisting rises through tower body reducer 1-4 into rectangular tower body, rectangular tower
Body cross section side length is 1.0-1.5 times of round tower body cross-sectional diameter, and flue gas actual internal area increases, flue gas flow rate decline,
Dust and fine mist are mutually collided poly- and are grown up, and partially fall to washing tower reactor, a small amount of droplet is carried in flue gas and passes through second level
Demister 1-5, flue gas flow area increase again, and flue gas flow rate continues to decline, and fine mist is polymerized to big drop and second level demisting
Device 1-5 plate-impact is captured, while the most of soluble-salt for being saturated the carrying of the drop in wet flue gas is removed.
Clean saturation wet flue gas after second level demister 1-5 demisting passes through liquid trap 1-6 and rises to condensate layer 1-7,
Cold liquid indirect heat exchange in condenser surface and Tube Sheet of Heat Exchanger cools down, and water recovery is at tiny liquid in cleaning saturation wet flue gas
Drop, is captured by condenser blade, falls to acquisition layer 1-6 collection, under the effect of gravity overflow to buffer tank 3.
The clean water of buffer tank 3 is delivered to 5 depth-type filtration of counter-infiltration system through high-pressure pump 4, and fresh water is delivered to fresh water storage
The conduct of case 6 is drunk and life water, concentrated water and buffer tank overflow water are delivered to equipment water storage tank and other facility water storage tanks,
Flap portion is with purification spraying layer 1-2 cleaning solution outlet ocean.
Wherein level-one demister 1-3 is one layer of baffle plate demister, and baffle(s) spacing 5mm-20mm, it is poor that import adjacent panels are grown
10mm-150mm, level-one demisting layer height are 0.2-1.0m；Second level demister 1-5 is removed using the ridge pattern that plate rearranges
Day with fog, second level demister are located at 1.0-1.5m, plate spacing 5-20mm, the high 0.5- of demister layer above tower body variable-diameter interface
2.0m。
The condenser heat exchange element that condensate layer 1-7 setting N (N≤4) layer is made of heat exchanger tube and baffling blade.Every layer of condensation
Device water inlet is individually connected with the outlet of coolant pump 2 supervisor by pipeline, and is set valve and individually controlled the cold flow quantity of heat exchanger, is adjusted
Saving flue-gas temperature reduces amplitude, realizes control condensing recovery yield, condensate liquid high in and low out in heat exchanger tube.Lower layer's condenser away from
Liquid trap 0.3-1.0m, adjacent two layers condenser spacing 0.3-0.8m, single layer condenser height 0.3-1.5m, single layer heat exchanger cigarette
Gas cooling extent is 0.5-3 DEG C.
When Drinking Water storage is sufficient, condenser water inlet pipe valve is adjusted, reduces condenser low temperature seawater flow,
Or reverse osmosis filtration system is closed, the clean water overflow that liquid trap 1-6 is collected is to buffer tank, by middle part overflow port overflow to outer
Discharge pipe, guarantee other equipment and facility are supplied with water.Ship power system load is low and the big storage of drinking water dosage is insufficient
When, condenser water inlet pipe valve is adjusted, low temperature seawater flow is increased, improves flue gas condensing amount and seawater yield.
Technical solution of the present invention and beneficial effect is described in detail in embodiment described above, it should be understood that
Above is only a specific embodiment of the present invention, it is not intended to restrict the invention, it is all to be done in spirit of the invention
Any modification, supplementary, and equivalent replacement etc., should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of device of low cost ship wet desulphurization tail gas preparing fresh, which is characterized in that including scrubbing tower, buffered water
Case, counter-infiltration system and fresh water storage tank；
The scrubbing tower lower sides or wash tower bottoms are equipped with gas inlet, and top is equipped with exhanst gas outlet, and bottom is equipped in tower
Leakage fluid dram；Purification spraying layer, level-one demisting layer, tower body are set gradually inside scrubbing tower and above gas inlet from the bottom to top
Reducer, second level demisting layer, acquisition layer and condensate layer；It is cylindrical void tower below the tower body reducer, top is pros
Shape void tower；
Water inlet is equipped at the top of the buffer tank, middle part is equipped with overflow port, and bottom is equipped with water outlet；The water inlet passes through pipe
The outlet on road and acquisition layer, the water outlet are connected to by high-pressure pump the import and export pipeline with counter-infiltration system water inlet；
Concentrated water outlet and the outer discharge pipe of the leakage fluid dram of the scrubbing tower, the overflow port of buffer tank and counter-infiltration system connect
It is logical.
2. the device of low cost ship wet desulphurization tail gas preparing fresh according to claim 1, which is characterized in that also wrap
Include coolant pump；
The purification spraying layer includes upper layer purification spraying layer and lower layer's purification spraying layer；
The water outlet pipeline of the coolant pump is divided into two-way, is connected to all the way by pipeline with the cooling liquid inlet of condensate layer, institute
The cooling liquid outlet for stating condensate layer purifies the spray liquid inlet communication of spraying layer by pipeline and lower layer；Another way by pipeline with
The spray liquid inlet communication of upper layer purification spraying layer.
3. the device of low cost ship wet desulphurization tail gas preparing fresh according to claim 1, which is characterized in that described
Demister in level-one demisting layer is baffle type mist eliminator, and the baffle type mist eliminator input end exhaust gases passes are greater than middle part
With outlet end exhaust gases passes.
4. the device of low cost ship wet desulphurization tail gas preparing fresh according to claim 1, which is characterized in that described
Demister in second level demisting layer is that the ridge type demister to be formed is arranged using plate.
5. the device of low cost ship wet desulphurization tail gas preparing fresh according to claim 1, which is characterized in that washing
In tower, the side length of upper section square tower body cross section is 1.0-1.5 times of the diameter of lower section circle tower body cross section.
6. the device of low cost ship wet desulphurization tail gas preparing fresh according to claim 1, which is characterized in that described
1~4 layer of condenser is set in condensate layer；The heat exchange element of condenser is made of heat exchanger tube and baffling blade.
7. the device of low cost ship wet desulphurization tail gas preparing fresh according to claim 6, which is characterized in that every layer
Condenser water inlet is individually connected with coolant pump outlet supervisor by pipeline, and is set valve and individually controlled the cold of every layer of condenser
But flow quantity.
8. a kind of method of low cost ship wet desulphurization tail gas preparing fresh, which comprises the following steps:
(1) ship tail gas is passed through in scrubbing tower by gas inlet, by seawater as purification spraying layer spray liquid to ship tail
Gas is washed, is cooled down, is humidified, and saturation wet flue gas is obtained；
(2) the saturation wet flue gas enters level-one demisting layer, removes partial particulate dust and saliferous droplet；
(3) after level-one demisting, wet flue gas enters top tower body through tower body reducer, into second level demisting layer, further removes
Granule dust and saliferous droplet obtain clean saturation wet flue gas；
(4) clean saturation wet flue gas passes through acquisition layer and rises to condensate layer, and cooling reaches hypersaturated state in condensate layer, wherein
Water recovery at liquid clean water and fall to acquisition layer, by acquisition layer outlet be discharged into buffer tank；Complete multi-stage condensing
Flue gas after receiving water is discharged by exhanst gas outlet；
(5) clean water is sent into counter-infiltration system by high-pressure pump, and fresh water and concentrated water are obtained after reverse osmosis membrane concentration.
9. the method for low cost ship wet desulphurization tail gas preparing fresh according to claim 8, which is characterized in that with low
Spray liquid of the warm seawater as the coolant liquid of condensate layer and upper layer purification spraying layer；High temperature seawater after being exchanged heat using condensate layer as
The spray liquid of lower layer's purification spraying layer.
10. the method for low cost ship wet desulphurization tail gas preparing fresh according to claim 8, which is characterized in that institute
The reverse osmosis membrane of counter-infiltration system is stated using tubular membrane；The operating pressure of reverse osmosis membrane is 2-10MPa, is discharged fresh water salt content <
0.05%.
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Cited By (2)
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| CN111558294A (en) * | 2020-05-27 | 2020-08-21 | 杭州蕴泽环境科技有限公司 | Wet flue gas purification system and method with energy-saving function |
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| CN110141928B (en) | 2022-03-01 |
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