WO2023021719A1 - 揮発アンモニアガス処理装置および処理方法 - Google Patents
揮発アンモニアガス処理装置および処理方法 Download PDFInfo
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- WO2023021719A1 WO2023021719A1 PCT/JP2021/047530 JP2021047530W WO2023021719A1 WO 2023021719 A1 WO2023021719 A1 WO 2023021719A1 JP 2021047530 W JP2021047530 W JP 2021047530W WO 2023021719 A1 WO2023021719 A1 WO 2023021719A1
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- ammonia gas
- ammonia
- unit
- volatilized
- mixing
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 292
- 238000000034 method Methods 0.000 title claims description 16
- 239000003054 catalyst Substances 0.000 claims abstract description 38
- 230000009467 reduction Effects 0.000 claims abstract description 35
- 239000000446 fuel Substances 0.000 claims abstract description 20
- 230000004308 accommodation Effects 0.000 claims abstract description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 84
- 238000002156 mixing Methods 0.000 claims description 56
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 30
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 22
- -1 ammonia compound Chemical class 0.000 claims description 16
- 239000013505 freshwater Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000004821 distillation Methods 0.000 claims description 13
- 239000002904 solvent Substances 0.000 claims description 9
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 6
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 6
- 239000013535 sea water Substances 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 description 27
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 24
- 239000002828 fuel tank Substances 0.000 description 21
- 239000007789 gas Substances 0.000 description 14
- 239000003638 chemical reducing agent Substances 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 12
- 239000007788 liquid Substances 0.000 description 12
- 238000003756 stirring Methods 0.000 description 8
- WTHDKMILWLGDKL-UHFFFAOYSA-N urea;hydrate Chemical compound O.NC(N)=O WTHDKMILWLGDKL-UHFFFAOYSA-N 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000001784 detoxification Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 231100000331 toxic Toxicity 0.000 description 3
- 230000002588 toxic effect Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000011514 reflex Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
- B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F21/00—Dissolving
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63H—MARINE PROPULSION OR STEERING
- B63H21/00—Use of propulsion power plant or units on vessels
- B63H21/38—Apparatus or methods specially adapted for use on marine vessels, for handling power plant or unit liquids, e.g. lubricants, coolants, fuels or the like
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
- F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
- F01N3/08—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous
Definitions
- the present invention relates to volatilized ammonia gas treatment.
- the volatilized ammonia gas is taken out, re-liquefied and returned to the tank.
- reliquefaction requires a large amount of electricity, which poses a problem from an energy efficiency point of view.
- diesel engines in particular use a selective reduction catalyst unit.
- the selective reduction catalyst unit removes nitrogen oxides generated by combustion of raw materials represented by heavy oil.
- a large amount of either urea water, ammonia gas, ammonia water, or an ammonia compound is required and stored in a tank.
- Patent Document 1 Japanese Patent Application Laid-Open No. 2018-204715 discloses a system and method for supplying boil-off gas generated from a liquefied gas fuel storage tank to gas utilization equipment by decompressing or compressing it. .
- Patent Document 1 requires a separate compressor and reservoir. Therefore, it is not possible to make effective use of the lines already installed on the ship. In particular, in LNH3-equipped ships, it is not possible to divert the reducing agent supply piping and the like to the selective reduction catalyst unit. In order to effectively use volatilized ammonia gas, it is necessary to increase the number of facilities.
- An object of the present invention is to provide a volatilized ammonia gas processing apparatus and a processing method that can effectively utilize volatilized ammonia gas.
- a first aspect of the present invention is An apparatus for the treatment of volatile ammonia gas on board ships carrying liquefied ammonia as cargo or engine fuel, comprising: a storage unit that stores ammonia gas volatilized from the liquefied ammonia; a transport unit that supplies the ammonia gas to a selective reduction catalyst unit connected to an engine of the ship; It is a volatilized ammonia gas treatment device.
- a second aspect of the present invention is An apparatus for the treatment of volatile ammonia gas on board ships carrying liquefied ammonia as cargo or engine fuel, comprising: a storage unit that stores ammonia gas volatilized from the liquefied ammonia; a transport unit that supplies the ammonia gas; a mixing unit that mixes the ammonia gas supplied from the transport unit and a solvent to generate an ammonia compound; a storage unit that stores the ammonia compound generated in the mixing unit; It is a volatilized ammonia gas treatment device.
- a third aspect of the present invention is A method of treating volatile ammonia gas on a vessel carrying liquefied ammonia as cargo or engine fuel, comprising: storing ammonia gas volatilized from the liquefied ammonia in a storage unit; supplying the ammonia gas stored in the storage unit to a selective reduction catalyst unit connected to the engine of the ship; It is a volatilized ammonia gas treatment method.
- a fourth aspect of the present invention is A method of treating volatile ammonia gas on a vessel carrying liquefied ammonia as cargo or engine fuel, comprising: storing ammonia gas volatilized from the liquefied ammonia in a storage unit; supplying the ammonia gas accommodated in the accommodation unit to the mixing unit; mixing the ammonia gas supplied to the mixing unit with a solvent to generate an ammonia compound; stockpiling the ammonia compound produced in the mixing unit; It is a volatilized ammonia gas treatment method.
- volatilized ammonia gas processing apparatus and processing method of the present invention volatilized ammonia gas can be effectively used.
- FIG. 1 is a schematic diagram of a volatilization ammonia gas treatment apparatus 1 of this embodiment.
- the volatilized ammonia gas treatment device 1 has a storage section 4 and a transport section 5 .
- the storage unit 4 stores volatilized ammonia gas generated from LNH3 stored in the ammonia fuel tank 2 and the cargo ammonia tank 3 .
- the transport section 5 directly supplies the ammonia gas to the selective reduction catalyst unit 10 as shown in FIG. 1 by using a blower or the like.
- the ammonia fuel tank 2 stores ammonia, which is part of the fuel used for the main engine of the marine engine. Ammonia is stored in the ammonia fuel tank 2 as LNH3. In order to maintain the liquid state of LNH3, the ammonia fuel tank 2 maintains the inside at high pressure or low temperature.
- the ammonia fuel tank 2 When a large amount of LNH3 is loaded on a ship for a long voyage or the like, the ammonia fuel tank 2 is thin and easy to work, and the full reflex type (atmospheric pressure type) or semi-reflex type (semi-pressurized type) is mainly used. Therefore, boil-off gas may be generated due to natural heat input or the like. Therefore, in order to maintain the ammonia fuel tank 2 in the liquid state of LNH3, a reliquefying device is required. The volatilized ammonia gas from the ammonia fuel tank 2 and the volatilized ammonia gas from the after-mentioned cargo ammonia tank 3 are transported to the storage unit 4 without going through the reliquefaction device.
- the cargo ammonia tank 3 stores LNH3 as cargo, not the fuel used for the main engine of the marine engine. Similar to the ammonia fuel tank 2, the cargo ammonia tank 3 maintains an internal high pressure or low temperature to maintain the liquid state of the LNH3 in the cargo ammonia tank 3.
- a full-reflex type (atmospheric pressure type) or a semi-reflex type (semi-pressurization type), which is thin and easy to process, is mainly used as the cargo ammonia tank 3 . Therefore, boil-off gas may be generated due to natural heat input or the like. Therefore, in order to maintain the cargo ammonia tank 3 with only LNH3, a reliquefaction device is required.
- a reliquefaction unit compresses or condenses the vaporized ammonia gas and thus requires a great deal of power.
- the volatilized ammonia gas from the cargo ammonia tank 3 and the volatilized ammonia gas from the ammonia fuel tank 2 are transported to the storage unit 4 without going through the reliquefaction device.
- the storage unit 4 stores volatilized ammonia gas from the ammonia fuel tank 2 and the cargo ammonia tank 3. As described above, the ammonia fuel tank 2 and cargo ammonia tank 3 are maintained at high pressure or low temperature so as to maintain the liquid state. However, volatilized ammonia gas, which is boil-off gas, may still be present. The volatilized ammonia gas is transported to the storage section 4 via a pressure reducing valve or the like. Pressure reducing valves and the like are provided above the ammonia fuel tank 2 and the cargo ammonia tank 3 .
- the transport section 5 of the present embodiment directly supplies the ammonia gas sent from the storage section 4 to the selective reduction catalyst unit 10 .
- the transport unit 5 has a transport function such as a blower. Thereby, ammonia gas can be supplied or transported through piping or the like.
- a transport function such as a blower.
- the material of the storage part 4 and the transport part 5 is preferably a corrosion-resistant material so as to prevent stress corrosion cracking.
- the transportation part 5 as a whole is not particularly limited as long as it is manufactured by a material and a welding method that are unlikely to cause stress corrosion cracking.
- the selective reduction catalyst unit 10 is a structure having a plurality of through holes extending in one direction to form gas flow paths.
- a catalyst is supported along the inner walls of the structure defining the through holes.
- vanadium, tungsten, and platinum are formed as contained elements.
- the catalyst may be produced by extrusion using titanium oxide as a main component.
- Exhaust gas containing nitrogen oxides emitted from a main engine of a marine engine or the like flows along the flow path. Nitrogen oxides are removed by supplying ammonia water as a reducing agent from the transport unit 5 at a predetermined flow rate and at a predetermined concentration.
- the selective reduction catalyst unit 10 is not particularly required only for diesel engines. If nitrogen oxides are also generated in a gas engine or the like, the selective reduction catalyst unit 10 is connected to the main engine or the like of the engine. Further, a flow rate adjusting section 7 may be provided before the selective reduction catalyst unit 10 .
- Ammonia is always used or stored in the main engines of marine engines that use ammonia as part of the fuel, and in ships that carry LNH3 as cargo. Therefore, urea water as a reducing agent, which is widely used when using a selective reduction catalyst, becomes unnecessary. Urea water and ammonia gas have substantially the same effect as reducing agents.
- ammonia gas As a reducing agent, it is possible to reduce the amount of carbon dioxide emitted while using the existing urea water supply piping. Specifically, after examining the pressure condition of the ammonia gas that satisfies the design conditions of the urea water supply pipe, the ammonia gas is supplied by a gas compressor or a pressure regulating valve. Therefore, a gate valve and a bypass line for the gas supply line may be provided before and after the liquid supply pump.
- the ammonia gas remaining in the upper part of the ammonia fuel tank 2 and cargo ammonia tank 3 can be used as it is as a reducing agent for the selective reduction catalyst.
- the space inside the ship can be effectively used.
- Ammonia is toxic, so a detoxification device is required, but the load on the detoxification device can also be reduced.
- the selective reduction catalyst unit 10 is not required only for diesel engines. Therefore, when the engine of the LNH3-equipped ship does not use ammonia as fuel, the volatilized ammonia gas is supplied to the selective reduction catalyst unit 10 from the cargo ammonia tank 3 . In this case, the type of engine is irrelevant. Similarly, when the main engine of the engine of the LNH3-equipped ship uses ammonia as fuel, the ammonia gas from either the ammonia fuel tank 2 or the cargo ammonia tank 3, or the ammonia gas mixed from both is selected. It is supplied to the reduction catalyst unit 10 .
- FIG. 2 is an overall view of the volatilized ammonia gas treatment apparatus 1 of this embodiment. Unlike the first embodiment, the ammonia gas stored in the storage section 4 from the ammonia fuel tank 2 or the cargo ammonia tank 3 is not directly supplied to the selective reduction catalyst unit 10 via the transport section 5 .
- the volatilized ammonia gas treatment apparatus 1 of this embodiment has a storage section 4 , a transport section 5 , a distillation section 6 , a mixing section 8 and a storage section 9 .
- the volatilized ammonia gas treatment device 1 may have a flow rate adjusting section 7 attached to the mixing section 8 .
- the ammonia gas stored in the storage section 4 from the ammonia fuel tank 2 or the cargo ammonia tank 3 is supplied to the lower portion of the mixing section 8 .
- the ammonia gas may be ammonia gas obtained by collecting the waste liquid emitted from the marine diesel engine itself, which uses ammonia as part of the fuel, and vaporizing the LNH3 separated therefrom.
- the distilling section 6 is for pumping up and distilling seawater located around the ship to obtain fresh water. Whether the ship is in operation or at berth, seawater located around the ship is taken up by pumps or the like. Fresh water is mainly used as cooling water for main engines, generator engines, and air compressors in marine diesel engines, and is also used as water supply to boilers, drinking water, and miscellaneous service water. As shown in FIG. 2, ammonia gas is dissolved in fresh water in the mixing unit 8 to produce aqueous ammonia.
- the flow rate adjusting section 7 is a flow rate adjusting valve.
- the flow rate adjusting section 7 adjusts the flow rate of liquid such as fresh water generated in the distillation section 6 .
- the flow rate adjusting unit 7 adjusts the flow rate of gas such as ammonia gas.
- the flow rate adjusting unit 7 is preferably installed at the inlet of the mixing unit 8 so that the ammonia water stored in the storage unit 9 has a predetermined concentration. Ammonia water having a predetermined concentration can be easily produced by the flow rate adjusting unit 7 . Further, the operation of the later-described stirring unit 91 can be omitted by the flow rate adjusting unit 7 .
- the mixing section 8 mixes the fresh water produced in the distillation section 6 with ammonia gas. Since ammonia gas is very soluble in water, it dissolves well in fresh water in a liquid state.
- the mixing section 8 has a shower head 81 in the upper part of the inside. shower head 81 sprays clean water produced in distillation section 6 .
- the ammonia gas which is lighter than air, dissolves in the fresh water in liquid form above. Ammonia water is thus stored in the lower portion of the mixing section 8 .
- ammonia gas is easily dissolved in water, it is not necessary to provide a stirring section in the mixing section 8 .
- the temperature of the water rises only to about 30 degrees.
- the temperature of the water rises to about 90°C due to the exothermic reaction due to the contact of water and ammonia gas.
- a heat exchanger (not shown) is installed in the mixing section 8 to remove the heat of reaction. By removing the heat of reaction between ammonia gas and water, temperature rise is prevented and the amount of dissolved ammonia gas increases. Also, it prevents the pressure rise in the mixing section 8 due to the temperature rise. This facilitates device design. Reaction heat generated by the reaction of ammonia gas with fresh water can also be used as energy for producing fresh water in the distillation section 6 .
- the mixing section 8 itself may be a heat exchanger type reactor such as a tubular reactor.
- the storage unit 9 stores the ammonia water produced by the mixing unit 8 .
- the storage unit 9 supplies ammonia water to the selective reduction catalyst unit 10 at a predetermined flow rate and a predetermined concentration. Therefore, it is preferable to install a densitometer or the like (not shown) at the inlet and outlet of the storage unit 9 .
- a first densitometer is provided at the inlet of the storage unit 9 .
- a second densitometer is provided at the outlet of the storage unit 9 .
- a density meter which is easier to measure than the densitometer, may be installed. In that case, it is necessary to acquire in advance the relationship between the measured value of the density meter and the concentration.
- the ammonia water concentration is about 15% at normal temperature and normal pressure.
- the ammonia water concentration is about 40% at maximum in a saturated state, and the higher the concentration of the ammonia water supplied to the selective reduction catalyst unit 10, the better.
- the storage unit 9 may have a stirring unit 91 inside.
- the aqueous ammonia supplied from the outlet of the mixing unit 8 to the storage unit 9 has a uniform concentration. However, due to the temperature gradient on the outer wall of the storage section 9, the ammonia gas may partially volatilize.
- the storage unit 9 may have a mechanism in its lower part for rotating the stirrer in one direction at a constant speed in the tank.
- the stirrer is, for example, rod-shaped, plate-shaped, or propeller-shaped.
- the stirring unit 91 is interlocked with concentration meters and density meters installed at the inlet and outlet of the storage unit 9 so as to supply ammonia water to the selective reduction catalyst unit 10 at a predetermined concentration and at a predetermined flow rate. preferably work.
- concentration difference between the inflow port and the outflow port of the storage unit 9 difference in concentration between the first densitometer and the second densitometer
- the storage unit 9 automatically activates the stirring unit 91 .
- the valve to the selective reduction catalyst unit 10 is not opened until the concentration difference falls within a certain value.
- the storage unit 9 automatically stops the stirring unit 91 and the valve to the selective reduction catalyst unit 10 is opened.
- the concentration of aqueous ammonia is made uniform in the pipes leading to the mixing unit 8 and the storage unit 9, and the like. If the concentration difference between the inflow port and the outflow port of the storage unit 9 is within a certain value, the stirring unit 91 becomes unnecessary.
- volatilization Ammonia gas can be temporarily stored in the storage unit 9 . As a result, the volatilized ammonia gas can be effectively used.
- the concentration of the aqueous ammonia is made uniform by the agitating section 91 located below the storage section 9 .
- ammonia water is supplied to the selective reduction catalyst unit 10 at a predetermined concentration and at a predetermined flow rate, and nitrogen oxides contained in the exhaust gas from the engine can be efficiently removed.
- FIG. 3 is an overall view of the volatilized ammonia gas treatment apparatus 1 of this embodiment. Unlike the second embodiment, the ammonia compound produced in the mixing section 8 is not directly supplied from the storage section 9 to the selective reduction catalyst unit 10 . Moreover, the solvent for the ammonia compound generated in the mixing section 8 of the present embodiment is clear water or sulfuric acid.
- Sulfuric acid is further supplied to the mixing section 8 of the present embodiment via the flow rate adjusting section 7 .
- the mixing section 8 mixes the supplied sulfuric acid and ammonia gas. Since ammonia gas is very soluble in water, it dissolves well in liquid sulfuric acid.
- the mixing section 8 has a shower head 81 in the upper part of the inside. The shower head 81 sprays sulfuric acid supplied to the mixing section 8 . This allows the ammonia gas, which is lighter than air, to dissolve into the liquid sulfuric acid above. Ammonium sulfate is thus stored in the lower portion of the mixing section 8 .
- the solvent for the ammonia compound is not limited to clear water or sulfuric acid.
- the storage unit 9 of the present embodiment stores and stores the aqueous ammonia or ammonium sulfate generated in the mixing unit 8 so as to be sold on land.
- a densitometer or the like is preferably installed at the inlet of the stockpile unit 9 so as to obtain a predetermined concentration so that the water can be used immediately after landing.
- a density meter may be installed at the inlet of the storage section 9 .
- ammonia gas vaporized from the ammonia fuel tank 2 and cargo ammonia tank 3 is toxic. Therefore, it is necessary to dispose of it using an abatement device. Unlike the second embodiment, which is not used for the selective reduction catalyst, in this embodiment, it is stored in the storage unit 9 so that it can be used on land. As a result, the ammonia compound can be used for sales or the like while reducing the load on the abatement device.
- the storage unit 9 will contain an ammonia compound (ammonia water and ammonium sulfate) can be temporarily stored. Therefore, it can be used in combination with applications such as sales on land and applications to supply the selective reduction catalyst unit 10 .
- ammonia gas volatilized from the ammonia fuel tank 2 and the cargo ammonia tank 3 may be stored in the storage section 4. Thereby, the load on the abatement device can be reduced.
- heat of reaction generated in the mixing section 8 by reaction of ammonia gas with fresh water may be used as energy for producing fresh water in the distillation section 6 .
- the mixing section 8 can be cooled at the same time as assisting the distillation section 6, so that environmental friendliness is high.
- the mixing section 8 itself may be a heat exchanger type reactor such as a tubular reactor in order to utilize reaction heat.
- the dashed lines in FIGS. 2 and 3 represent the flow of reaction heat.
- Ammonia water is stored in the lower portion of the mixing section 8 . Therefore, it is preferable to install a heat exchanger or the like in the lower portion of the mixing section 8 so that the heat of chemical reaction can be used more easily.
- a sensor for measuring nitrogen oxides is attached to the lower portion of the selective reduction catalyst unit 10 of the second embodiment, and the flow rate of the aqueous ammonia supplied from the storage unit 9 may be adjusted by feedback control. Even if the concentration of discharged nitrogen oxides varies depending on the operating conditions of the engine, the amount of ammonia water supplied from the storage unit 9 can be adjusted, so that the apparatus can be made more efficient with high environmental adjustment. Alternatively, the concentration of the ammonia water generated in the mixing unit 8 and supplied to the storage unit 9 may be adjusted instead of the amount of ammonia water supplied from the storage unit 9 . Again, the total amount of reducing agent required for the removal of nitrogen oxides is supplied to the selective reduction catalyst unit 10 . In particular, it is preferable to adjust the concentration of the ammonia water supplied to the storage unit 9 in a situation where the storage unit 9 does not store much ammonia water.
Abstract
Description
一方、船舶に用いられるエンジンのうち、特にディーゼルエンジンでは、選択式還元触媒ユニットが用いられる。選択式還元触媒ユニットは、重油に代表される原料の燃焼により発生する窒素酸化物を除去する。還元剤として、尿素水またはアンモニアガス、アンモニア水、アンモニア化合物のいずれかが大量に必要となり、タンクに備蓄される。
貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理装置であって、
前記液化アンモニアから揮発するアンモニアガスを収容する収容部と、
前記アンモニアガスを前記船舶のエンジンに接続される選択式還元触媒ユニットに供給する輸送部と、
を有する、揮発アンモニアガス処理装置である。
貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理装置であって、
前記液化アンモニアから揮発するアンモニアガスを収容する収容部と、
前記アンモニアガスを供給する輸送部と、
前記輸送部から供給された前記アンモニアガスと、溶媒とを混合して、アンモニア化合物を生成する混合部と、
前記混合部で生成された前記アンモニア化合物を備蓄する備蓄部と、
を有する、揮発アンモニアガス処理装置である。
貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理方法であって、
前記液化アンモニアから揮発するアンモニアガスを収容部に収容し、
前記収容部に収容された前記アンモニアガスを前記船舶のエンジンに接続される選択式還元触媒ユニットに供給する、
揮発アンモニアガス処理方法である。
貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理方法であって、
前記液化アンモニアから揮発するアンモニアガスを収容部に収容し、
前記収容部に収容された前記アンモニアガスを混合部に供給し、
前記混合部に供給された前記アンモニアガスと、溶媒とを混合して、アンモニア化合物を生成し、
前記混合部で生成された前記アンモニア化合物を備蓄する、
揮発アンモニアガス処理方法である。
本実施形態の揮発アンモニアガス処理装置1の構成について説明する。
図1は、本実施形態の揮発アンモニアガス処理装置1の概略図である。揮発アンモニアガス処理装置1は、収容部4と、輸送部5とを有する。収容部4は、アンモニア燃料タンク2と貨物用アンモニアタンク3に貯留されたLNH3から発生する揮発アンモニアガスを収容する。輸送部5は、アンモニアガスをブロワー等により、図1のように、選択式還元触媒ユニット10に直接供給する。
収容部4には、再液化装置を経由せず、貨物用アンモニアタンク3からの揮発アンモニアガスとアンモニア燃料タンク2からの揮発アンモニアガスが輸送される。
選択式還元触媒に液体状態の還元剤を供給する場合、気化させる必要があるところ、本実施形態では、輸送部5を介して、気体状態のアンモニアガスを選択式還元触媒ユニット10に供給するため、還元剤を気化させる手間を省略できる。
なお、輸送部5は、全体として、応力腐食割れ発生しにくい材質や溶接方法で製造されていれば、特に限定されるものではない。
また、選択式還元触媒ユニット10の手前に、流量調整部7が設けられてもよい。
同様に、LNH3搭載船のエンジンの主機等がアンモニアを燃料とする場合は、アンモニア燃料タンク2及び貨物用アンモニアタンク3のいずれか一方からのアンモニアガスや、両方から混合したアンモニアガスが、選択式還元触媒ユニット10に供給される。
以下、第2実施形態について説明する。なお、第1実施形態と略同様の機能や構成については、その説明を省略する。
図2は、本実施形態の揮発アンモニアガス処理装置1の全体図である。第1実施形態と異なり、アンモニア燃料タンク2や貨物用アンモニアタンク3から収容部4に収容されたアンモニアガスは、輸送部5を介して選択式還元触媒ユニット10に直接供給されない。本実施形態の揮発アンモニアガス処理装置1は、収容部4と、輸送部5と、蒸留部6と、混合部8と、備蓄部9とを有する。揮発アンモニアガス処理装置1は、混合部8に取り付けられる流量調整部7を有してもよい。本実施形態において、アンモニア燃料タンク2や貨物用アンモニアタンク3から収容部4に収容されたアンモニアガスは、混合部8の下部に供給される。
流量調整部7は、備蓄部9に蓄えられるアンモニア水が所定の濃度となるように、混合部8の入口に設置されることが好ましい。流量調整部7により、所定の濃度のアンモニア水が作成しやすい。また、流量調整部7により、後述の撹拌部91での動作を省略できる。
なお、アンモニアガスは水に溶けやすいため、混合部8に撹拌部を設けなくてもよい。
なお、反応熱を利用するため、混合部8自体をチューブラーリアクターといった熱交換器型反応器としてもよい。
なお、濃度計よりも計測することが容易な密度計が設置されてもよい。その場合、密度計の計測値と濃度との関係を予め取得しておくことが必要となる。例えば、光計測での密度計で0.912という数値になっている場合、アンモニア水濃度は、常温常圧で約15%程度となる。アンモニア水濃度は、飽和状態で最大で40%程度であり、選択式還元触媒ユニット10に供給されるアンモニア水の濃度は高いほど好ましい。
以下、第3実施形態について説明する。なお、第1実施形態、第2実施形態と略同様の機能や構成については、その説明を省略する。
図3は、本実施形態の揮発アンモニアガス処理装置1の全体図である。第2実施形態と異なり、混合部8で生成されたアンモニア化合物は、備蓄部9から選択式還元触媒ユニット10に直接供給されない。また、本実施形態の混合部8において生成されるアンモニア化合物の溶媒は、清水又は硫酸である。
なお、アンモニア化合物の溶媒は、清水や硫酸に限られるものではない。
第1~第3実施形態の揮発アンモニアガス処理装置1に関して、以下のような態様を採用してもよい。
これにより、除害装置への負荷を低減できる。
これにより、蒸留部6へのアシストと当時に、混合部8を冷却できるため、環境調和性が高い。
また、備蓄部9でのアンモニア水の供給量ではなく、混合部8で生成され、備蓄部9に供給されるアンモニア水の濃度を調整してもよい。この場合も、窒素酸化物の除去に必要とされる還元剤の総量が、選択式還元触媒ユニット10に供給される。特に、備蓄部9にアンモニア水があまり貯留されていない状況において、備蓄部9に供給されるアンモニア水の濃度を調整することが好ましい。
2 アンモニア燃料タンク
3 貨物用アンモニアタンク
4 収容部
5 輸送部
6 蒸留部
7 流量調整部
8 混合部
81 シャワーヘッド
9 備蓄部
91 撹拌部
10 選択式還元触媒ユニット
Claims (12)
- 貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理装置であって、
前記液化アンモニアから揮発するアンモニアガスを収容する収容部と、
前記アンモニアガスを前記船舶のエンジンに接続される選択式還元触媒ユニットに供給する輸送部と、
を有する、揮発アンモニアガス処理装置。 - 貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理装置であって、
前記液化アンモニアから揮発するアンモニアガスを収容する収容部と、
前記アンモニアガスを供給する輸送部と、
前記輸送部から供給された前記アンモニアガスと、溶媒とを混合して、アンモニア化合物を生成する混合部と、
前記混合部で生成された前記アンモニア化合物を備蓄する備蓄部と、
を有する、揮発アンモニアガス処理装置。 - 海水から清水を蒸留する蒸留部を更に有し、
前記混合部は、前記蒸留部で蒸留された前記清水と、前記輸送部から供給された前記アンモニアガスとを混合して、アンモニア水を生成する、
請求項2に記載の揮発アンモニアガス処理装置。 - 前記混合部は、前記混合部に供給される硫酸と、前記輸送部から供給された前記アンモニアガスとを混合して、硫酸アンモニウムを生成する、
請求項2又は3に記載の揮発アンモニアガス処理装置。 - 前記収容部は、前記エンジン燃料の供給ラインから揮発する前記アンモニアガスを収容する、
請求項1~4のいずれかに記載の揮発アンモニアガス処理装置。 - 前記蒸留部は、前記混合部にて発生する熱を利用する、
請求項3~5のいずれかに記載の揮発アンモニアガス処理装置。 - 貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理方法であって、
前記液化アンモニアから揮発するアンモニアガスを収容部に収容し、
前記収容部に収容された前記アンモニアガスを前記船舶のエンジンに接続される選択式還元触媒ユニットに供給する、
揮発アンモニアガス処理方法。 - 貨物又はエンジン燃料として液化アンモニアを搭載する船舶における揮発アンモニアガスの処理方法であって、
前記液化アンモニアから揮発するアンモニアガスを収容部に収容し、
前記収容部に収容された前記アンモニアガスを混合部に供給し、
前記混合部に供給された前記アンモニアガスと、溶媒とを混合して、アンモニア化合物を生成し、
前記混合部で生成された前記アンモニア化合物を備蓄する、
揮発アンモニアガス処理方法。 - 蒸留部が海水から清水を蒸留し、
前記混合部に供給された前記アンモニアガスと、前記蒸留部で蒸留された前記清水とを混合して、アンモニア水を生成する、
請求項8に記載の揮発アンモニアガス処理方法。 - 前記混合部に硫酸を供給し、
前記混合部に供給された前記硫酸と前記アンモニアガスとを混合して、硫酸アンモニウムを生成する、
請求項8又は9に記載の揮発アンモニアガス処理方法。 - 前記収容部が、前記エンジン燃料の供給ラインから揮発する前記アンモニアガスを収容する、
請求項7~10のいずれかに記載の揮発アンモニアガス処理方法。 - 前記混合部にて発生する熱を利用して、前記海水から前記清水を蒸留する、
請求項9~11のいずれかに記載の揮発アンモニアガス処理方法。
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