KR102231449B1 - Apparatus for reducing greenhouse gas emission in vessel and vessel including the same - Google Patents

Abstract

The present invention relates to a device for reducing the emissions of greenhouse gasses of a ship, which increases CO_2 removal efficiency, and a ship having the same. The device of the present invention comprises: a seawater supply unit (110) for supplying seawater; an ammonia water producing unit (120) for producing and supplying ammonia water; an absorption tower (130) having a CO_2 removal unit (133) formed therein; and an ammonia regenerating unit (140).

Description

Vessel's greenhouse gas emission reduction device and ship equipped with it {APPARATUS FOR REDUCING GREENHOUSE GAS EMISSION IN VESSEL AND VESSEL INCLUDING THE SAME}

The present invention NO _X and SO _X and the CO ₂ separation discharge to IMO greenhouse gases to meet the emission regulations, SO _X to remove the CO ₂ after removing the CO ₂ solubility with CO ₂ removing efficiency from the exhaust gas discharged from ship engines It relates to an apparatus for reducing greenhouse gas emissions of a ship and a ship having the same.

Recently, global warming and related environmental disasters have occurred due to the influence of greenhouse gas emissions caused by indiscriminate use of fossil fuels.

Accordingly, a series of technologies related to the capture and storage of carbon dioxide, which is a representative greenhouse gas, do not emit carbon dioxide capture and storage (CCS) technology, which has recently attracted great attention. Among CCS technologies, chemical absorption is It is the most commercialized technology among them in terms of being capable of large-scale processing.

In addition, carbon dioxide emissions regulation for regulation through the EEDI of the IMO, in 2050 and aims to more than 50% reduction of 2008 emissions in 2030 should reduce the 40% of 2008 emissions because it does not emit CO ₂ In addition, the technology to capture the _{emitted CO 2 is attracting attention.}

For reference, among the CCS technologies that directly capture and store carbon dioxide, the CO ₂ capture technology can _{be approached in various ways depending on the CO 2} generation conditions of the target process. Currently, representative technologies are absorption method, adsorption method, and membrane separation method. The wet absorption method has high technical maturity in onshore plants and is the closest capture technology to commercialization of CCS technology due _{to its high technical maturity and easy mass treatment of CO 2. As absorbents, amines and ammonia are mainly used.}

On the other hand, the aforementioned technology to reduce the emission of carbon dioxide or to capture the generated carbon dioxide is currently not commercialized in ships, and a method using hydrogen or ammonia as a fuel is currently being developed and is at the stage of commercialization. It wasn't too early.

In particular, in ships equipped with a scrubber to use high sulfur oil, the solubility of _{SO X} is large, so it is first changed into a compound of _{NaSO 3} , so it is difficult to remove _{CO 2 until all SO X} is dissolved. have.

_{Therefore, for ships using fossil fuels, it is necessary to apply a technology for converting and discharging CO 2} out of the exhaust gas emitted from the ship's engine into a material that does not affect the environment, or converting it into a useful material and storing it on the ship. Is raised.

Korean Registered Patent Publication No. 2031210 (Ship exhaust gas reduction device and pollutant removal method, 2019.10.11) Korean Registered Patent Publication No. 1201426 (Greenhouse gas reduction device for ships, 2012.11.14)

The technical problem to be achieved by the idea of the present invention is to meet IMO greenhouse gas emission regulations by separating and discharging _{NO X} , SO _X and CO _{2 from exhaust gas, and removing SO X} and then CO ₂ to remove CO ₂ solubility and CO 2 _{2 It} improves removal efficiency, reduces the _{cost of NH 3} regeneration by using _{Ca(OH) 2} , reduces the size of the capacity at the rear end of the membrane filter, and consumes only _{NH 3} and Ca(OH) ₂ when removing _{CO 2} It is to provide a ship's greenhouse gas emission reduction device and a ship equipped with the same, which can reduce the removal cost.

In order to achieve the above object, the present invention, a seawater supply unit for supplying seawater; An ammonia water production unit that reacts fresh water and NH _{3 to prepare and supply ammonia water;} The exhaust gas discharged from the ship engine is cooled by reacting with seawater supplied from the seawater supply unit, and the cooled exhaust gas and the ammonia water from the ammonia water production unit are reacted _{to convert CO 2} into NH ₄ HCO ₃ (aq). CO ₂ removal portion for removing the CO ₂ formed, absorption tower; _{And the NH 4} HCO ₃ (aq) discharged from the absorption tower reacts with Ca(OH) _{2 to regenerate NH 3} and return to the ammonia water production unit for supply, an ammonia regeneration unit; including, greenhouse gas emission of ships Provide a reduction device.

In addition, the absorption tower further includes a NOx absorption unit for absorbing and removing NOx of exhaust gas discharged from the ship engine, and cooling the exhaust gas from which the NOx has been removed by reacting with seawater supplied from the seawater supply unit. The cooled exhaust gas and the ammonia water from the ammonia water production unit are reacted _{to convert CO 2} into NH ₄ HCO ₃ (aq) _{to remove CO 2} , and the ammonia regeneration unit regenerates NH ₃ to remove the ammonia water production unit and the NO. _It can be supplied by returning to the X absorber.

In addition, the absorption tower further comprises an SOx absorption unit for dissolving and removing SOx while reacting and cooling the exhaust gas discharged from the ship engine with seawater supplied from the seawater supply unit, and the exhaust gas from which the SOx has been removed and the by reacting the ammonia from the ammonia production unit may switch the CO ₂ to the NH ₄ HCO ₃ (aq) to remove the CO _2.

_{In addition, the absorption tower, a NO X} absorption unit for absorbing and removing _{NO X} from the exhaust gas discharged from the ship engine _{, and cooling by reacting the exhaust gas from which the NO X} is removed with seawater supplied from the seawater supply unit. SO _X absorbing part which dissolves and removes SO _{X , and converts CO 2} to NH ₄ HCO ₃ (aq) by _{reacting the exhaust gas from which SO X} is removed and ammonia water from the ammonia water production part to remove _{CO 2} The CO ₂ removal unit may be stacked, and the ammonia regeneration unit _{may regenerate NH 3} and return to the ammonia water production unit and the NO _X absorption unit to be supplied.

In addition, the seawater supply unit, a seawater pump that receives seawater from the outside of the ship through a sea chest and _{pumps it to the SO X absorption unit;} And a control valve that adjusts the flow rate of seawater supplied from the seawater pump according to the amount of exhaust gas.

In addition, the ammonia water production unit, a fresh water tank for storing fresh water; A fresh water pump for pumping and supplying fresh water from the fresh water tank; A tower tank, an NH ₃ spray nozzle formed at the bottom of the tower tank _{to inject NH 3} upward, a fresh water spray nozzle formed at the top of the tower tank to spray fresh water from the fresh water pump downward, and the NH ₃ Ammonia water production tower comprising a filler formed between the spray nozzle and the fresh water spray nozzle to contact _{fresh water and NH 3 to dissolve NH 3} to generate ammonia water, and a cooling jacket that cools heat generation of the tower tank due to the dissolution reaction; And an ammonia water pump for supplying ammonia water to the upper end of _{the CO 2} removal unit from an ammonia water storage tank for storing the ammonia water drained to the lower end of the ammonia water production tower.

In addition, the ammonia water production tower may further include a mist removal plate formed in a curved multi-plate shape on the top of the tower tank to return mist scattered from fresh water in the direction of the filler.

_{In addition, an NH 3 supply pipe for supplying NH 3} exhausted from the upper end of the ammonia water production tower to the lower end of _{the CO 2} removal unit may be further included.

In addition, the filler may be configured in multiple stages of distillation column packing, which is designed to have a large contact area per unit volume.

In addition, a solution redistributor may be further formed between the distillation column packings configured in multiple stages.

In addition, the diameter and height of the tower tank may be designed such that the flow _{rate of fresh water and the flow rate of NH 3 are 1/2 of the overflow rate.}

Further, when the above the NH ₃ from the ammonia regeneration unit supplied through the ammonia production part NH ₃ injection nozzles, or loss, and lack of NH ₃ is to supply the NH ₃ from a separate NH ₃ storage tank to compensate for the losses and deficiencies can do.

In addition, the NO _{X absorbing unit directly receives NH 3} from the ammonia regeneration unit through a blower or a compressor through the first NH ₃ injection nozzle, or supplies urea water from the urea water storage tank when _{NH 3 is insufficient.} It can be supplied to _{the second NH 3} injection nozzle through the pump to compensate for the shortfall.

In addition, the SO _X absorption unit may include a multi-stage seawater injection nozzle connected to the control valve to inject seawater downward.

In addition, a porous upper plate in which a flow path through which exhaust gas passes is formed is formed under the seawater injection nozzle in multiple stages, so that seawater and exhaust gas may contact each other.

Furthermore, the absorber in the lower water spray nozzle, a filling material which is water and exhaust gas into contact filled is formed, the sea water can be to dissolve the SO _X.

In addition, the SO _X absorbing part may include an umbrella-shaped partition wall covering the exhaust gas inlet pipe so that the washing water does not flow backward.

In addition, the CO ₂ removal unit, an ammonia water injection nozzle connected to the ammonia water pump to inject ammonia water downward; A filler for converting _{CO 2} into NH ₄ HCO ₃ (aq) by contacting CO ₂ with aqueous ammonia; A cooling jacket formed in multiple stages for each section of the absorption tower filled with the filler to cool heat generated by the _{CO 2 removal reaction;} Water spray that does not react with CO _{2 and collects NH 3 discharged to the outside;} A mist removal plate formed in a curved multi-plate shape to return ammonia water in the direction of the filler; A partition wall formed to prevent ammonia water from flowing back; And an umbrella-shaped blocking plate covering the exhaust gas inlet hole of the partition wall.

In addition, the absorption tower may _{further include an EGE formed between the NO x} absorption portion and the SO _x absorption portion to exchange heat between waste heat of the ship engine and boiler water.

In addition, an auxiliary boiler that receives a mixture in the form of heat-exchanged steam and saturated water, separates the steam and supplies it to a steam consumer, a boiler water circulating water pump that circulates and supplies boiler water from the auxiliary boiler to the EGE, and consumes the steam. It may include a cascade tank for recovering the condensed water condensed from the wife, and a supply pump and a control valve for controlling and supplying the amount of boiler water from the cascade tank to the auxiliary boiler.

In addition, Ca (OH) ₂ storage tank for the ammonia reproducing unit, stores the Ca (OH) _2; A mixing tank for generating _{CaCO 3} (s) and H _{2 O by stirring NH 4} HCO ₃ (aq) and Ca(OH) ₂ discharged from the absorption tower with a stirrer, _{and regenerating NH 3} (g); _{A membrane filter for separating CaCO 3} (s) and fresh water by sucking the solution and precipitate from the mixing tank; A high pressure pump for transferring the solution and precipitate to the membrane filter at high pressure; _{And a CaCO 3} (s) storage tank _{for storing CaCO 3} (s) in a slurry or solid state.

In addition, fresh water separated by the membrane filter may be supplied to the ammonia water production unit, or fresh water additionally generated by the mixing tank relative to the total circulating fresh water may be stored in the fresh water tank.

In addition, in the Ca(OH) _{2 storage tank, Ca(OH) 2} may be produced by reacting fresh water supplied from the fresh water tank with CaO.

In addition, a washing water tank that stores washing water discharged from the absorption tower, a filtering unit that adjusts turbidity to meet the outboard discharge conditions of the washing water transferred by the transfer pump to the washing water tank, and a neutralizing agent for pH adjustment are injected. A water treatment device having a unit, and a sludge storage tank configured to separate and store solid discharges may further include a discharge unit.

On the other hand, the present invention can provide a ship equipped with the above-listed greenhouse gas emission reduction device.

_{According to the present invention, NO X} , SO _X and CO ₂ from the exhaust gas exhausted from the ship engine are converted into substances that do not affect the environment so as to meet the IMO greenhouse gas emission regulations and discharged separately or converted into useful substances for storage. And, after removing _{SO X , CO 2} is removed to increase CO ₂ solubility and CO ₂ removal efficiency, and by using _{Ca(OH) 2 , NH 3} regeneration cost can be reduced, and the capacity size of the rear end of the membrane filter can be reduced. In addition, only relatively inexpensive NH ₃ and Ca(OH) _{2 are consumed when removing CO 2} , so that the removal cost can be reduced, and side reactions caused by SO _{X remaining during NH 3} regeneration are eliminated so that impurities are not included when recovering ammonia. There is an effect that can be.

1 shows a schematic configuration diagram of an apparatus for reducing greenhouse gas emissions of a ship according to an embodiment of the present invention.
FIG. 2 is a circuit diagram of a system implementing the apparatus for reducing greenhouse gas emissions of the ship of FIG. 1.
3 is a separate view of the seawater supply unit of the apparatus for reducing greenhouse gas emission of the ship of FIG. 2.
Figure 4 is a separate view showing the ammonia water production unit of the greenhouse gas emission reduction device of the ship of Figure 2.
5 is a separate view showing the absorption tower of the apparatus for reducing greenhouse gas emission of the ship of FIG. 2.
6 is a separate diagram illustrating an SO _X absorber of the absorption tower of FIG. 5.
7 is a separate view showing the steam generating unit of the greenhouse gas emission reduction device of the ship of FIG. 2.
FIG. 8 is a separate view showing an ammonia regeneration unit and an ammonia water production unit of the apparatus for reducing greenhouse gas emission of the ship of FIG.
9 illustrates various fillers applied to the apparatus for reducing greenhouse gas emissions of the ship of FIG. 2.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those of ordinary skill in the art may easily implement the present invention. The present invention may be implemented in various different forms and is not limited to the embodiments described herein.

The apparatus for reducing greenhouse gas emissions of a ship according to an embodiment of the present invention includes a seawater supply unit that supplies seawater, an ammonia water production unit that produces and supplies ammonia water by reacting _{fresh water and NH 3, and the exhaust gas discharged from the ship engine to seawater.} A CO _{2 removal unit that removes CO 2 by reacting with seawater supplied from the supply unit to cool it, and converts CO 2} to NH ₄ HCO ₃ (aq) by reacting the cooled exhaust gas with the ammonia water from the ammonia water production unit is formed, absorption _{The tower and the NH 4} HCO ₃ (aq) discharged from the absorption tower is reacted with Ca(OH) _{2 to regenerate NH 3} and return to the ammonia water production unit for supply, and an ammonia regeneration unit is included.

At this time, depending on the type and specification of the engine (low pressure engine or high pressure engine) and the type of fuel supplied to the engine (HFO, MDO, MGO, LNG, ammonia, etc.), the absorption tower selectively includes a NOx absorber or a SOx absorber, or , Can be configured to include all.

In particular, with respect to the SOx absorption unit, as described later, since SOx can be dissolved by reacting with seawater, cooling of exhaust gas and absorption of SOx can be performed at once.

On the other hand, a ship according to another embodiment of the present invention may provide a ship equipped with the aforementioned device for reducing greenhouse gas emissions from the ship.

Hereinafter, an embodiment in which the NOx absorber, the SOx absorber, and the CO ₂ remover are stacked on the absorption tower is described, but is not limited thereto. As described above, the NOx absorber and/or the SOx absorber depends on the type of engine and fuel. It can be determined whether to be equipped accordingly.

The apparatus for reducing greenhouse gas emission of a ship according to an embodiment of the present invention includes, as a whole, a seawater supply unit 110 for supplying seawater, an ammonia water production unit 120 for manufacturing and supplying ammonia water by reacting _{fresh water and NH 3, and a ship engine} The exhaust gas discharged from (10) is cooled by reacting with seawater supplied from the seawater supply unit 110, and the cooled exhaust gas and the ammonia water from the ammonia water production unit 120 are reacted to convert _{CO 2} into NH _{4 HCO 3} (aq ) by converting it to a CO ₂ removal unit 133 is formed, the absorption tower 130, and the NH ₄ HCO ₃ (aq), the Ca (OH) ₂ (aq) discharged from the absorption tower 130 to remove the CO ₂ IMO greenhouse by separating and discharging _{NO X} , SO _X and CO ₂ from exhaust gas, including ammonia regeneration unit 140, which reacts with _{and regenerates NH 3} (g) and returns to the ammonia water production unit 120 for supply. The main idea is to meet gas emission regulations, remove CO _{2 after removing SO X} to increase CO ₂ removal efficiency, and eliminate side reactions caused by SO _{X remaining during NH 3} regeneration so that impurities are not included when recovering ammonia. do.

Hereinafter, with reference to FIGS. 1 to 9, the configuration of the above-described vessel's greenhouse gas emission reduction apparatus will be described in detail as follows.

First, the seawater supply unit 110 supplies seawater to the SO _X absorption unit 132 of the absorption tower 130, specifically, as shown in FIGS. 2 and 3, a sea chest (sea chest) ( The flow rate of seawater supplied from the seawater pumps 111a and b according to the amount of exhaust gas and the seawater pumps 111a and b _{that sucks seawater and pumps it to the SO X} absorption unit 132 is supplied through (not shown). It may be composed of a control valve 112 to control. Here, the seawater pumps 111a and b may be composed of a suction pump 111a that sucks seawater from the outside of the ship and a seawater transfer pump 111b that pumps and transports _{seawater to the SO X absorption unit 132.} have.

For reference, depending on the ship's berthing or sailing, it may be selectively supplied to the seawater pumps 111a and b from a high sea chest that sucks seawater from the top or a low sea chest that sucks seawater from the bottom according to the depth of the ship. That is, when the ship is berthing, the upper seawater is clean rather than the lower seawater, so the high sea chest is used, and when the ship is sailing, the lower seawater is cleaner than the upper seawater, so the low seachest can be used.

Here, the control valve 112 may be a manually operated diaphragm valve or a solenoid type valve that controls the flow rate of seawater, but is not limited thereto, and the amount of seawater injection through the seawater injection nozzle 132a according to the amount of exhaust gas Any type of valve can be applied as long as it can be adjusted.

Next, the ammonia water production unit 120 _{reacts fresh water and NH 3} supplemented when regenerated or insufficient to produce and supply ammonia water (NH ₄ OH(aq)).

Specifically, as shown in Figures 2 and 4, the ammonia water production unit 120, a fresh water tank 121 for storing fresh water, a fresh water pump for pumping and supplying fresh water from the fresh water tank 121 122, tower tank (123a), and a tower tank (123a) is formed at the bottom is formed at the top of the NH ₃ injection nozzles (123b) and the tower tank (123a) for injecting NH ₃ into the upper clean water pump 122 fresh water to fresh water injection nozzle (123c) for spraying downwardly from, and is formed between the NH ₃ injection nozzles (123b) and the fresh water injection nozzle (123c) was dissolved NH ₃ contacting the fresh water with NH ₃ to produce aqueous ammonia Ammonia water production tower 123 composed of a filler 123d and a cooling jacket 123e that cools heat generation of the tower tank 123a due to the dissolution reaction according to the following [Chemical Formula 1], and ammonia water production Ammonia water pump 124 that supplies ammonia water from the ammonia water storage tank 124a that stores the ammonia water drained to the lower end of the tower 123 to the ammonia water spray nozzle 133a formed on the upper end of the _{CO 2 removal unit 133} It can be made of.

Here, the fresh water tank 121 is distilled water produced on board or fresh water separated by the membrane filter 144, that is, a mixing tank 143 compared to the total circulating fresh water required for _{generation of ammonia water and regeneration of NH 3 and} Fresh water that is additionally generated by passing through the membrane filter 144 may be stored (see FIG. 8 ).

On the other hand, the ammonia water production tower 123, referring to FIG. 4, is formed in a curved multi-plate shape on the top of the upper fresh water spray nozzle 123c of the tower tank 123a, and contains a mist scattered from the fresh water with a filler 123d. ), so that fresh water can be discharged to the outside through the exhaust gas, so that the mist collides with the bend and the droplet becomes larger, so that it is drained in the direction of the lower filler 123d. can do.

_{In addition, it further includes an NH 3 supply pipe (123g) that supplies NH 3} (g) exhausted to the upper end of the ammonia water production tower 123 to the lower end of the _{CO 2} removal unit 133, so that excess NH that is not dissolved and exhausted ₃ (g) may be absorbed by the ammonia water flowing through the _{CO 2} removal unit 133 to minimize the loss of _{NH 3.}

On the other hand, the amount of NH ₃ regenerated by the ammonia water regeneration unit 140 generates ammonia water by the ammonia water production tower 123 or is supplied to _{the first NH 3 injection nozzle 131b of the NO x} absorption unit 131. As the result is insufficient, when a shortage of _{NH 3 occurs or a loss of NH 3} itself occurs, a separate NH ₃ storage tank 123h may be provided _{to supply NH 3} to compensate for the loss and shortfall. _{That is, the NH 3} injection nozzle 123b of the ammonia water production unit 120 from the ammonia regeneration unit 140, or the first NH ₃ injection nozzle _{of the NO X} absorption unit 131 through a blower 131a or a compressor (131b) when the supply of NH _3, or direct, the loss or lack of NH ₃ may be received from the NH ₃ supplying the NH ₃ storage tank (123h) so as to substitute for the loss or deficiency.

In addition, the diameter and height of the tower tank (123a) _{is preferably designed so that the flow rate of fresh water and the flow rate of NH 3} are 1/2 of the flooding velocity, through which the NH ₃ injection nozzle (123b) is Through the NH ₃ is injected at a pressure slightly higher than the normal pressure, it is possible to offset the pressure drop in the wet state of the tower tank (123a).

In addition, the filler 123d may be configured in multiple stages of distilling column packing, which is designed to have a large contact area per unit volume, and in consideration of the contact area per unit area and the pressure drop and overflow rate of gas, FIG. 9 A distillation column packing suitable for the process as illustrated in can be selected.

Meanwhile, a solution redistributor (not shown) is formed between the distillation column packings configured in multiple stages, so that channeling of fresh water can be prevented.

In addition, the ammonia water pump 124 is configured as a centrifugal pump, and can effectively supply a large amount of ammonia water by pumping a large amount of ammonia water from the ammonia _{water production tower 123 to the CO 2 removal unit 133.}

In addition, the cooling jacket 123e may be cooled so that the reaction temperature of the dissolution reaction is maintained at 30°C to 50°C in consideration of the solubility _{of NH 3.}

_{Next, the absorption tower 130, as shown in Figs. 2 and 5, a NO x} absorption unit that absorbs and removes _{NO x} from exhaust gas discharged from the ship engine 10 of the main engine or power generation engine ( 131) and _{the SO X} absorption unit 132 that dissolves and removes _{SO X} while reacting and cooling the exhaust gas from which _{NO X} has been removed with seawater, and supplied from the exhaust gas and ammonia water production unit 120 from which _{SO X has been removed.} by reacting the ammonia be converted to CO ₂ by NH ₄ HCO ₃ (aq) and CO ₂ removal unit 133 to remove the CO ₂ is formed laminated in the vertical direction, and absorb the NO _X and SO _X and CO ₂ in order To remove it.

Here, the absorption tower 130 may be configured to include a NO _X absorption unit 131, an SO _X absorption unit 132, a CO ₂ removal unit 133 and an EGE 134 to be described later, and each individual module It may be configured to be modularized and combined, or may be integrated and configured in a single tower form, and the absorption tower 130 itself may be configured as a single tower or a plurality of towers.

Specifically, the NO _X absorption unit 131 is a SCR (Selective Catalyst Reactor), and directly supplies _{NH 3 from the ammonia regeneration unit 140 to the first NH 3} injection nozzle 131b through a blower 131a or a compressor, or , When the NH ₃ is insufficient, the urea water (UREA) of the urea water storage tank 131c is supplied to the second NH ₃ injection nozzle 131e through the urea water supply pump 131d and may be replaced to compensate for the shortage. .

Here, when the decomposition the number of elements, so that NH ₃ and CO ₂ occurs by supplying NH ₃ directly to the top of the can and, NO _X absorbent 131 may be desirable to reduce the CO ₂ emissions, the NO detecting the NO _X concentration _{An X} sensor can be formed.

In addition, the SO _X absorption unit 132 is a section in primary contact with seawater, and is connected to the control valve 112 and is composed of a multistage seawater injection nozzle 132a that injects seawater downward to dissolve _{SO X and} While removing the dust of (soot), the temperature of the exhaust gas through the seawater injection nozzle (132a) or a separate cooling jacket (not shown _{) is required by the CO 2} removal unit 133 to 27 ℃ to 33 ℃, preferably , It can be cooled to around 30℃.

On the other hand, as shown in Figure 6 (a), under the seawater injection nozzle (132a), a porous upper plate (132b) in which a flow path through which exhaust gas passes is formed is formed in multiple stages, respectively, so that seawater and exhaust gas are smoothly Or, as shown in (b) of FIG. 6, under the seawater injection nozzle 132a, absorption towers 132c filled with fillers for contacting seawater and exhaust gas are formed, respectively, so that seawater SO _X It can also be made to dissolve.

On the other hand, in _{order to further increase the solubility of SO X} , a compound that forms alkali ions, such as a basic chemical of NaOH or MgO, may be incorporated into a closed loop system.

For reference, the closed-loop system entails consumption of additional basic chemicals, but has the advantage of having a small amount of circulating seawater, and the open-loop system that discharges _{dissolved SO X outboard by spraying only seawater consumes additional basic chemicals.} Since there is no and simple advantage, it can be configured as a hybrid system combining open and closed circuits.

Thus, hayeoseo to subsequently remove the CO ₂ from the CO ₂ removal unit 133 after removal of the SO _X first through the SO _X absorbing part 132, the first with a compound such as the solubility of SO _X cursor Na ₂ SO ₃ It is possible to improve the solubility of CO _{2 and the removal efficiency of CO 2} by solving the problem that it is difficult to remove _{CO 2} until all _{SO X is dissolved.}

Here, the washing water is drained to a discharge section 160 by the SO _X absorbing part 132, the SO ₃ ^- the ionic compound other than, SO ₄ ^2-, suit, NaSO _3, NaSO _4, MgCO _3, and MgSO ₄ It is included together, and the SO _X absorbing part 132 is an umbrella-shaped partition wall covering the exhaust gas inlet pipe 132d so that the _{washing water does not flow back to the NO X absorbing part 131 or the EGE 134 (} 132e).

In addition, the CO ₂ removal unit 133, as shown in Figure 5, is connected to the ammonia water pump 124 and the ammonia water spray nozzle (133a) for spraying the ammonia water downward, and the CO ₂ and the ammonia water to contact the following _{The filler (133b) converting CO 2} into NH ₄ HCO ₃ (aq) according to [Formula 2] and the absorption tower filled with the filler (133b) are formed in multiple stages to cool the heat generated by the _{CO 2 removal reaction.} A cooling jacket (not shown) to be maintained at 30℃ to 50℃, _{a water spray (133c) that collects NH 3} discharged to the outside without reacting with _{CO 2,} and a bent multi-plate shape to contain ammonia water as a filler ( A mist removal plate 133d returning in the direction of 133b), _{a partition wall 133e formed so that ammonia water does not flow back to the SO X} absorption unit 132, and an exhaust gas inlet hole 133e-1 of the partition wall 133e. ) May be configured as an umbrella-shaped blocking plate (133f) covering.

Here, the CO ₂ removal unit 133 _{reacts and removes the exhaust gas from which NO X} and SO _X has been previously removed, and ammonia water, so that _{side reactions due to NO X} and SO _X do not occur during the _{CO 2} removal process, thereby preventing the generation of impurities. Since it can be minimized, NH ₄ HCO ₃ with less impurities can be obtained in a subsequent process.

In addition, the filler 133b may be configured in multiple stages of distillation column packing, designed to have a large contact area per unit volume, and as illustrated in FIG. 9 in consideration of the contact area per unit area and the pressure drop and overflow rate of the gas. A distillation column packing suitable for the process can be selected.

On the other hand, the absorption tower 130 _{is formed between the NO X} absorption unit 131 and the SO _X absorption unit 132 to exchange heat between the waste heat of the ship engine 10 and the boiler water EGE (Exhaust Gas Economizer) 134 It may further include.

Next, the ammonia regeneration unit 140 reacts NH ₄ HCO ₃ (aq) discharged from the absorption tower 130 with Ca(OH) ₂ to regenerate NH _{3 so} that the ammonia water production unit 120 and the NO _X absorption unit ( 131) and supply and reuse, and store or discharge _{CO 2} in the _{form of CaCO 3 (s).}

Specifically, as shown in FIGS. 2 and 8, the ammonia regeneration unit 140, Ca (OH) CO ₂ in the Ca (OH) ₂ a storage tank 141, the absorption tower 130, which stores the _two agents _{NH 4} HCO ₃ (aq) and Ca(OH) ₂ discharged from the rejection 133 are stirred with a stirrer 142 to generate _{CaCO 3} (s) and H ₂ O by the following [Chemical Formula 3], and NH _{3 A membrane filter 144 that separates CaCO 3} (s) and fresh water by suctioning solution and precipitate from the mixing tank 143 to regenerate (g), and the solution and precipitate to a membrane the high pressure pump 145 and the slurry or CaCO ₃ for storing the CaCO ₃ (s) in the solid state to transfer to a high pressure to the filter (144) (s) may comprise a storage tank (not shown).

_{Here, NH 4} HCO ₃ (aq) and Ca(OH) ₂ are continuously reacted by a stirrer 142 installed in the mixing tank 143, but a constant temperature is maintained to facilitate the reaction.

On the other hand, the fresh water separated by the membrane filter 144 is supplied to the fresh water spray nozzle 123c of the ammonia water production unit 120, or to the mixing tank 143 compared to the total circulating fresh water required for the _{generation of ammonia water and NH 3 regeneration.} By storing the fresh water additionally generated in the fresh water tank 121, waste of fresh water can be eliminated.

In addition, in the Ca(OH) _{2 storage tank 141, Ca(OH) 2} may be generated by reacting fresh water supplied from the fresh water tank 121 with CaO.

Therefore, when NaCl saturated aqueous solution or seawater is used, it contains a large amount of water, dilutes the concentration of ammonia water, _{and increases the cost of NH 3} regeneration. Unlike using saturated NaCl aqueous solution or seawater, only _{CaO or Ca(OH) 2 is relatively inexpensive.} There is no need to add water by inputting, there is no reduction in the concentration of ammonia water, it is possible to reduce the size of the capacity of the membrane filter 144, and it is possible to reduce the cost of _{NH 3 regeneration.} That is, in theory, only CaO is consumed, and NH ₃ and fresh water are reused, so that the _{cost of removing CO 2} can be considerably reduced.

In addition, the membrane filter 144 sucks the solution and sediment from the mixing tank 143 and transfers NaHCO ₃ and other by-product sediment at high pressure by the high pressure pump 145 _{to separate fresh water and CaCO 3} to a solid state. Store or discharge outboard.

_{In addition, NH 3} regenerated by the mixing tank 143 is supplied to _{the NH 3} injection nozzle 123b of the ammonia water production unit 120 and the first NH _{3 injection nozzle 131b of the NO X} absorption unit 131 to provide ammonia water. By reusing it for manufacturing and NO _X removal, it is possible to save cost by minimizing the consumption of relatively expensive NH _3.

Next, as shown in FIG. 7, the steam generator 150 receives a mixture in the form of steam and saturated water heat-exchanged through the EGE 134 and receives a steam drum (not shown). The auxiliary boiler 151 that separates the steam and supplies it to the steam consumer, the boiler water circulating water pump 152 that circulates and supplies the boiler water from the auxiliary boiler 151 to the EGE 134, and the steam consumption. A cascade tank 153 that recovers the condensed water that has been condensed and changed phase after being condensed, and a supply pump 154 and a control valve that regulates and supplies the amount of boiler water from the cascade tank 153 to the auxiliary boiler 151 Consist of (155), it generates and supplies steam necessary for heating equipment on board the ship.

Here, when the load of the ship's engine 10 is large, the amount of heat that can be provided from the exhaust gas is high and the amount of steam required in the ship can be sufficiently produced through the EGE 134, but if not, the auxiliary boiler 151 itself The fuel can also be burned to produce the necessary steam.

Next, the discharge unit 160, as shown in Figure 2, the washing water tank 161 for storing the washing water discharged from the absorption tower 130, the washing water tank 161 to the transfer pump 162 A water treatment device 163 having a filtering unit for adjusting turbidity to meet the outboard discharge conditions of the washing water transferred by the filter unit and a neutralizing agent injection unit for pH control, and a sludge storage tank for separating and storing solid discharges such as chutes ( 164), the washing water that passes through the water treatment device 163 and satisfies the outboard discharge conditions is discharged outboard, and solid discharges such as chutes that do not meet the outboard discharge conditions are separately stored in the sludge storage tank 164 Can be stored.

On the other hand, NaOH may be exemplified as a neutralizing agent for meeting the outboard discharge conditions, but it is assumed that the substances discharged from the absorption tower 130 are both acidic or basic, and can neutralize each of these acids or basics as necessary. A neutralizing agent may be selected and used.

Therefore, by the configuration of the ship's GHG emission reduction device as described above, NO _X , SO _X and CO ₂ from the exhaust gas exhausted from the ship engine are not affected to the environment so as to meet the IMO GHG emission regulations. It is converted into a substance and discharged separately or it is stored by converting it into a useful substance. After removing _{SO X , CO 2} is removed to increase CO ₂ solubility and CO ₂ removal efficiency, and use _{Ca(OH) 2} to reduce the cost of _{NH 3 regeneration.} can and, it is possible to reduce the capacity size portion rear end membrane filter, it is possible to reduce the CO ₂ removed in a relatively inexpensive NH ₃ and Ca (OH) ₂ removal is consumed only the cost, due to the SO _X remaining playback NH ₃ to By removing side reactions, impurities may not be included when recovering ammonia.

In the above, the present invention has been described with reference to the embodiments shown in the drawings. However, the present invention is not limited thereto, and various modifications or other embodiments falling within the scope equivalent to the present invention are possible by those of ordinary skill in the art. Therefore, the true scope of protection of the present invention should be determined by the claims that follow.

110: seawater supply unit 111a,b: seawater pump
112: control valve 120: ammonia water manufacturing unit
121: fresh water tank 122: fresh water pump
123: ammonia water production tower 124: ammonia water pump
130: absorption tower 131: NO _X absorption part
132: SO _X absorption part 133: CO _{2 removal part}
134: EGE 140: ammonia regeneration unit
141: Ca(OH) ₂ storage tank 142: stirrer
143: mixing tank 144: membrane filter
145: high pressure pump 150: steam generator
151: auxiliary boiler 152: boiler water circulation water pump
153: cascade tank 154: supply pump
155: control valve 160: discharge part
161: washing water tank 162: transfer pump
163: water treatment device 164: sludge storage tank
10: ship engine

Claims (25)

Seawater supply unit for supplying seawater;
An ammonia water production unit that reacts fresh water and NH _{3 to prepare and supply ammonia water;}
The exhaust gas discharged from the ship engine is cooled by reacting with seawater supplied from the seawater supply unit, and the cooled exhaust gas and the ammonia water from the ammonia water production unit are reacted _{to convert CO 2} into NH ₄ HCO ₃ (aq). CO ₂ removal portion for removing the CO ₂ formed, absorption tower; And
Including; an ammonia regeneration unit for regenerating NH _{3 by reacting NH 4} HCO ₃ (aq) discharged from the absorption tower with Ca(OH) ₂ and returning to the ammonia water production unit for supplying;
Vessel's greenhouse gas emission reduction device. The method of claim 1,
The absorption tower further includes a NOx absorption unit for absorbing and removing NOx of exhaust gas discharged from the ship engine, and cooling the exhaust gas from which the NOx is removed by reacting with seawater supplied from the seawater supply unit. The exhaust gas and the ammonia water from the ammonia water production unit are reacted _{to convert CO 2} into NH ₄ HCO ₃ (aq) to remove _{CO 2,}
The ammonia regeneration unit regenerates NH ₃ and returns to the ammonia water production unit and the NO _{X absorption unit for supply,}
Vessel's greenhouse gas emission reduction device. The method of claim 1,
The absorption tower further includes an SOx absorption unit for dissolving and removing SOx while reacting and cooling the exhaust gas discharged from the ship engine with seawater supplied from the seawater supply unit,
By reacting the ammonia from the SOx removing the exhaust gas and the ammonia production unit to convert the CO ₂ to the NH ₄ HCO ₃ (aq) to remove CO _2,
Vessel's greenhouse gas emission reduction device. The method of claim 1,
_{The absorption tower includes a NO X} absorbing unit that absorbs and removes _{NO X} from the exhaust gas discharged from the ship engine _{, and SO X while cooling by reacting the exhaust gas from which the NO X} has been removed with seawater supplied from the seawater supply unit. by converting the SO _X absorbing portion that was removed by dissolution, by reacting the ammonia from the SO _X is to remove exhaust gas and the ammonia production unit the CO ₂ in _{NH 4 HCO 3 (aq) CO} 2 to remove CO ₂ The removal portion is formed by lamination,
The ammonia regeneration unit regenerates NH ₃ and returns to the ammonia water production unit and the NO _{X absorption unit for supply,}
Vessel's greenhouse gas emission reduction device. The method according to claim 3 or 4,
The seawater supply unit,
A seawater pump that receives seawater from the outside of the ship and _{pumps it to the SO X absorption unit;} And
Characterized in that it comprises; a control valve that adjusts the flow rate of seawater supplied from the seawater pump according to the amount of exhaust gas,
Vessel's greenhouse gas emission reduction device. The method according to any one of claims 1 to 4,
The ammonia water production unit,
A fresh water tank for storing fresh water;
A fresh water pump for pumping and supplying fresh water from the fresh water tank;
A tower tank, an NH ₃ spray nozzle formed at the bottom of the tower tank _{to inject NH 3} upward, a fresh water spray nozzle formed at the top of the tower tank to spray fresh water from the fresh water pump downward, and the NH ₃ Ammonia water production tower comprising a filler formed between the spray nozzle and the fresh water spray nozzle to contact _{fresh water and NH 3 to dissolve NH 3} to generate ammonia water, and a cooling jacket that cools heat generation of the tower tank due to the dissolution reaction; And
And an ammonia water pump for supplying ammonia water to the upper end of _{the CO 2} removal unit from an ammonia water storage tank for storing the ammonia water drained to the lower end of the ammonia water production tower.
Vessel's greenhouse gas emission reduction device. The method of claim 6,
The ammonia water production tower,
It characterized in that it further comprises a mist removal plate formed in the shape of a curved multi-plate above the tower tank to return mist scattered from fresh water in the direction of the filler,
Vessel's greenhouse gas emission reduction device. The method of claim 6,
Further comprising the NH ₃ supply pipe for supplying the NH ₃ that is discharged from the upper end of the tower to the bottom of the ammonia produced in the CO ₂ removal,
Vessel's greenhouse gas emission reduction device. The method of claim 6,
The filler,
Designed to have a large contact area per unit volume, characterized in that the distillation column packing is configured in multiple stages,
Vessel's greenhouse gas emission reduction device. The method of claim 9,
Characterized in that the solution redistributor is further formed between the distillation column packing consisting of multiple stages,
Vessel's greenhouse gas emission reduction device. The method of claim 6,
The diameter and height of the tower tank,
It is characterized in that the flow rate of fresh water and the flow rate of NH ₃ are designed to be 1/2 of the overflow rate,
Vessel's greenhouse gas emission reduction device. The method of claim 6,
When the above the NH ₃ from the ammonia regeneration unit supplied through the ammonia production part NH ₃ injection nozzles, or loss, and lack of NH ₃ is to supply the NH ₃ from a separate NH ₃ storage tank that to compensate for losses and deficiencies Characterized by,
Vessel's greenhouse gas emission reduction device. The method according to claim 2 or 4,
The NO _X absorbing part,
_{NH 3} is directly supplied from the ammonia regeneration unit to the first NH ₃ injection nozzle through a blower or a compressor, or when NH ₃ is insufficient, the urea water from the urea water storage tank is injected with _{the second NH 3 through the urea water supply pump.} Characterized in that to compensate for the deficit by being supplied to the nozzle,
Vessel's greenhouse gas emission reduction device. The method of claim 5,
The SO _X absorbing part,
It characterized in that it comprises a multi-stage seawater injection nozzle for injecting seawater downwardly connected to the control valve,
Vessel's greenhouse gas emission reduction device. The method of claim 14,
In the lower portion of the seawater injection nozzle, a porous upper plate having a flow path through which the exhaust gas passes is formed in multiple stages, respectively, so that the seawater and the exhaust gas come into contact with each other,
Vessel's greenhouse gas emission reduction device. The method of claim 14,
An absorption tower filled with a filler for allowing seawater and exhaust gas to contact each other is formed under the seawater injection nozzle, so that the seawater dissolves _{SO X,}
Vessel's greenhouse gas emission reduction device. The method of claim 14,
The SO _X absorbing part,
It characterized in that it comprises an umbrella-shaped partition wall covering the exhaust gas inlet pipe so that the washing water does not flow back,
Vessel's greenhouse gas emission reduction device. The method of claim 6,
The CO ₂ removal unit,
An ammonia water spray nozzle connected to the ammonia water pump to spray ammonia water downward;
A filler for converting _{CO 2} into NH ₄ HCO ₃ (aq) by contacting CO ₂ with aqueous ammonia;
A cooling jacket formed in multiple stages for each section of the absorption tower filled with the filler to cool heat generated by the _{CO 2 removal reaction;}
Water spray that does not react with CO _{2 and collects NH 3 discharged to the outside;}
A mist removal plate formed in a curved multi-plate shape to return ammonia water in the direction of the filler;
A partition wall formed to prevent ammonia water from flowing back; And
Characterized in that it comprises; an umbrella-shaped blocking plate covering the exhaust gas inlet hole of the partition wall,
Vessel's greenhouse gas emission reduction device. The method of claim 4,
The absorption tower,
It characterized in that it further comprises an EGE formed between the NO _X absorbing part and the SO _X absorbing part to exchange heat between waste heat of the ship engine and boiler water,
Vessel's greenhouse gas emission reduction device. The method of claim 19,
An auxiliary boiler that receives a mixture in the form of heat-exchanged steam and saturated water, separates the steam and supplies it to a steam consumer, a boiler water circulating water pump that circulates and supplies boiler water from the auxiliary boiler to the EGE, and from the steam consumer It characterized in that it further comprises a cascade tank for recovering the condensed condensed water, and a steam generator comprising a supply pump and a control valve for adjusting and supplying the amount of boiler water from the cascade tank to the auxiliary boiler,
Vessel's greenhouse gas emission reduction device. The method of claim 6,
The ammonia regeneration unit,
Ca (OH) Ca (OH) 2 storage tank for storing the _two;
A mixing tank for generating _{CaCO 3} (s) and H _{2 O by stirring NH 4} HCO ₃ (aq) and Ca(OH) ₂ discharged from the absorption tower with a stirrer, _{and regenerating NH 3} (g);
_{A membrane filter for separating CaCO 3} (s) and fresh water by sucking the solution and precipitate from the mixing tank;
A high pressure pump for transferring the solution and precipitate to the membrane filter at high pressure; And
CaCO ₃ (s) storage tank for storing a slurry or in solid form CaCO ₃ (s); in that it comprises a characterized,
Vessel's greenhouse gas emission reduction device. The method of claim 21,
Supplying the fresh water separated by the membrane filter to the ammonia water production unit, or storing the fresh water additionally generated by the mixing tank relative to the total circulating fresh water in the fresh water tank,
Vessel's greenhouse gas emission reduction device. The method of claim 22,
In the Ca(OH) ₂ storage tank, characterized in that _{Ca(OH) 2} is produced by reacting fresh water supplied from the fresh water tank with CaO,
Vessel's greenhouse gas emission reduction device. The method according to any one of claims 1 to 4,
A washing water tank for storing the washing water discharged from the absorption tower, a filtering unit for adjusting turbidity to meet the outboard discharge condition of the washing water transferred by the transfer pump to the washing water tank, and a neutralizing agent injection unit for pH adjustment. It characterized in that it further comprises a discharge unit, consisting of a water treatment device provided, and a sludge storage tank for separating and storing solid discharges,
Vessel's greenhouse gas emission reduction device. A ship equipped with a GHG emission reduction device of a ship according to any one of claims 1 to 4.

Images