KR102231448B1 - Apparatus for reducing greenhouse gas emission in vessel and vessel including the same - Google Patents

Abstract

The present invention relates to an apparatus for reducing emission of greenhouse gas of a ship, which increases the CO_2 removal efficiency, and to a ship having the same. The apparatus 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) in which an NO_X absorption unit (131), an SO_X absorption unit (132), and a CO_2 removal unit (133) are stacked; and an ammonia regeneration unit (140).

Description

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

The invention and the NO _X and SO _X and CO ₂ from the exhaust gas separating discharge to meet the IMO greenhouse gas emission regulations, after removing the SO _X to remove CO ₂ to increase the CO ₂ solubility and CO ₂ removal efficiency, It relates to a ship's greenhouse gas emission reduction device and a ship equipped with 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 of using hydrogen or ammonia as 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. 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 Increases removal efficiency, reduces the _{cost of NH 3} regeneration by using NaCl solid powder, reduces the size of the device at the rear end of the membrane filter, _{and consumes only NH 3} and Ca(OH) ₂ when removing _{CO 2,} resulting in removal cost. It is to provide a device for reducing greenhouse gas emissions of a ship and a ship equipped with it.

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 formed remover to remove CO _2, absorption tower; _{And NH 4} HCO ₃ (aq) discharged from the absorption tower is sequentially reacted with NaCl (s) and Ca (OH) _{2 to regenerate NH 3} and return to the ammonia water production unit for supplying, an ammonia regeneration unit; including; It provides an apparatus for reducing greenhouse gas emissions of ships.

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 includes a NO x} absorption unit that absorbs and removes _{NO x} from the exhaust gas discharged from the ship engine, and the exhaust gas from which _{the NO x} has been removed is reacted with seawater supplied from the seawater supply unit to cool the SO. convert the SO _X absorbing component to remove by dissolving the _X, the SO _X is by reacting the ammonia from the exhaust gas and the ammonia production unit to remove CO ₂ to the NH ₄ HCO ₃ (aq) and CO to remove the CO _{2 2 The} 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 supplying the ammonia water drained to the lower end of the ammonia water production tower to the upper end of the CO _{2 removal unit.}

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 to 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, designed to have a large contact area per unit volume, may be configured in multiple stages of distillation column packing.

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.}

In addition, through the blower or the compressor from the ammonia regeneration unit the NH ₃ supply the NH ₃ to the spray nozzle directly, or at the time of shortage of NH ₃ can be to replace the deficiency by supplying NH ₃ from a separate NH ₃ storage tanks .

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 2nd NH 3} injection nozzle through a pump to replace 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 _{washing water does not flow back to the NO X absorbing part.}

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 further include a cascade tank for recovering the condensed water condensed from the wife, and a steam generating unit including a supply pump and a control valve for adjusting and supplying the amount of boiler water from the cascade tank to the auxiliary boiler.

In addition, the ammonia regeneration unit may include a NaCl silo for storing and supplying NaCl solid powder; A mixing tank for generating _{NaHCO 3} (s) and NH _{4 Cl by stirring NH 4} HCO ₃ (aq) and NaCl(s) discharged from the absorption tower with a stirrer; Membrane filter to remove the NH ₄ Cl to the suction NaHCO ₃ (s) and NH ₄ Cl from the mixing tank; A high pressure pump for transferring a mixture of NaHCO ₃ (s) and NH _{4 Cl to the membrane filter at high pressure; NaHCO 3} storage tank for storing _{NaHCO 3} in a slurry or solid state; Ca (OH) Ca (OH) 2 storage tank for storing the _two; And NH ₃ regeneration tank for regenerating _{NH 3 by reacting NH 4} Cl and Ca(OH) ₂ with a stirrer.

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. It may further include a discharge unit, including a water treatment device having a unit, and a sludge storage tank for separating and storing solid discharges.

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

According to the present invention, NO _X , SO _X and CO ₂ are separated and discharged from exhaust gas to meet IMO greenhouse gas emission regulations, and _{CO 2} is removed after _{SO X is removed to increase CO 2} solubility and CO ₂ removal efficiency, Using NaCl solid powder, _{it is possible to reduce the cost of regeneration of NH 3} , reduce the size of the device at the rear end of the membrane filter, _{and only consume NH 3} and Ca(OH) ₂ when removing _{CO 2} to reduce the removal cost. _{NaHCO 3} with little impurities can be stored as a solid, and side reactions caused by SO _{X remaining during NH 3} regeneration can be removed, so that impurities are not included when recovering ammonia.

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 showing 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 of an ammonia regeneration unit of the apparatus for reducing greenhouse gas emissions of the ship of FIG. 2.
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 for supplying seawater, an ammonia water production unit for producing and supplying ammonia water by reacting _{fresh water and NH 3, and exhaust gas discharged from a ship engine.} by reaction with the supplied water from the water supply cooling, and reacting the ammonia from the cooled exhaust gas and the ammonia production unit CO ₂ to NH ₄ converted to HCO ₃ (aq) and CO ₂ formed remover to remove CO _2, It includes an absorption tower, and an ammonia regeneration unit that sequentially reacts _{NH 4} HCO ₃ (aq) discharged from the absorption tower with NaCl(s) and Ca(OH) _{2 to regenerate NH 3} and return to the ammonia water production unit for supply. .

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 may optionally include a NOx absorber or a SOx absorber. , 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 SOx absorption can be performed at once.

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 or not to be equipped accordingly.

The apparatus for reducing greenhouse gas emissions 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, and exhaust exhaust from the ship engine 10 and SO _X absorbing component 132, which while the NO _X absorbing portion 131 for removing and absorbing NO _X in the gas, NO _X is an exhaust gas removing cooling is reacted with water to remove by dissolving the SO _X, SO _X The absorption tower is formed by stacking the CO _{2 removal unit 133 for removing CO 2} by reacting the removed exhaust gas with the ammonia water from the ammonia water production unit 120 _{to convert CO 2} into NH ₄ HCO ₃ (aq) 130), and the NH ₄ HCO ₃ (aq) discharged from the absorption tower 130 sequentially reacts with NaCl(s) and Ca(OH) _{2 to regenerate NH 3} to absorb the ammonia water production unit 120 and NO _X Including the ammonia regeneration unit 140 that is returned to the unit 131 and supplied, NO _X , SO _X and CO ₂ are separated and discharged from the exhaust gas to meet the IMO greenhouse gas emission regulations, and after removing _{SO X, CO 2} is removed to increase the efficiency of _{CO 2} removal, and side reactions caused by SO _{X remaining during NH 3} regeneration are removed so that impurities are not included when recovering ammonia.

Hereinafter, with reference to FIGS. 1 to 9, the configuration of the above-described vessel's greenhouse gas emission reduction device 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) ( A seawater pump 111 that sucks seawater and pumps it to the SO _X absorption unit 132 through (not shown), and a control valve that adjusts the flow rate of seawater supplied from the seawater pump 111 according to the amount of exhaust gas. It can be composed of 112.

For reference, it is possible to selectively supply to the seawater pump 111 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, depending on the ship's berthing or sailing. 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 sailed, 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} to prepare and supply ammonia water (NH _{4 OH).}

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 It may be made of an ammonia water pump 124 supplying 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.}

Here, the fresh water tank 121 may store distilled water produced on board.

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 to disperse the mist scattered from the fresh water in the direction of the filler 123d. By further including a revolving mist removal plate 123f, fresh water can be discharged to the outside through exhaust gas, so that the mist collides with the bend and the droplet becomes large, 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 into the ammonia water flowing from the _{CO 2} removal unit 133 to minimize the loss of _{NH 3.}

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.}

_{In addition, NH 3} is directly supplied from the ammonia regeneration unit 140 to the NH ₃ injection nozzle 123b through a blower 125 or a compressor, or when the NH ₃ is insufficient, a separate pressure gauge valve 126 is used. It is also possible to replace the shortfall by receiving _{NH 3} from an NH ₃ storage tank (not shown).

_{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), _{the SO X} absorption unit 132 dissolving and removing _{SO X while reacting and cooling the exhaust gas from which NO X} has been removed with seawater, and the exhaust gas _{from which SO X} has been removed and the ammonia water production unit 120. A CO _{2 removal unit 133 that removes CO 2} by reacting with ammonia water to _{convert CO 2} into NH ₄ HCO ₃ (aq) is stacked in a vertical direction to sequentially absorb _{NO X} , SO _X and CO ₂ Remove.

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 directly supplied with NH 3} from the ammonia regeneration unit 140 to the first NH ₃ injection nozzle 131b through the blower 131a or the compressor, or when NH ₃ is insufficient The urea water (UREA) of the urea water storage tank 131c may be supplied to the second NH ₃ injection nozzle 131e through the urea water supply pump 131d to replace the shortfall.

_{Here, since NH 3} and CO ₂ are generated when the urea water is decomposed, it may be desirable to reduce the amount of _{CO 2} generated by directly supplying _{NH 3.}

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 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 drained to the discharge unit 160 by the _{SO X absorption unit 132 contains SO 3} -, SO ₄ ^2- , chute, NaSO ₃ , NaSO ₄ , MgCO ₃ , MgSO ₄ and other ionic compounds. 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 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 ammonia water to contact the following [Chemical Formula 2] or [Formula 3] ] By _{the filler (133b) converting CO 2} into NH ₄ HCO ₃ (aq) and the absorption tower filled with the filler (133b) is formed in multiple stages to cool the heat generated by the _{CO 2 removal reaction from 30℃ to} A cooling jacket (not shown) to maintain the temperature at 50°C, _{a water spray (133c) that collects NH 3} discharged to the outside without reacting with _{CO 2,} and a curved multi-plate shape to provide ammonia water in the direction of the filler (133b) Covers a mist removal plate 133d to be returned to, _{a partition wall 133e formed so that ammonia water does not flow back to the SO X} absorber 132 and an exhaust gas inlet hole 133e-1 of the partition wall 133e It may be composed of an umbrella-shaped blocking plate (133f).

Here, the CO ₂ removal unit 133 _{reacts the exhaust gas from which NO X} and SO _X has been previously removed with ammonia water, so _{that side reactions do not occur during the CO 2} removal process, thus minimizing the generation of impurities. NaHCO ₃ can be obtained.

In addition, the filler 133b may be configured in a multi-stage 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 sequentially reacts the NH ₄ HCO ₃ (aq) discharged from the absorption tower 130 with NaCl(s) and Ca(OH) _{2 to regenerate the NH 3 so} that the ammonia water production unit 120 ) And _{return to the NO X} absorption part 131 to be supplied and reused.

Specifically, as shown in FIGS. 2 and 8, the ammonia regeneration unit 140 includes a NaCl silo 141 for storing and supplying NaCl solid powder, and NH _{4 discharged from the absorption tower 130.} HCO ₃ (aq) and NaCl (s) supplied from the NaCl silo 141 were stirred with a stirrer 142, and the precipitates NaHCO ₃ (s) and NH ₄ Cl (aq) were prepared by the following [Chemical Formula 4] and a mixing tank (143) for generating, with a membrane filter (membrane filter) (144) separating the NH ₄ Cl with suction NaHCO ₃ (s) and NH ₄ Cl from the mixing tank 143, NaHCO ₃ (s) and A high-pressure pump 145 that transfers a mixture of NH ₄ Cl at high pressure to the membrane filter 144, a NaHCO ₃ storage tank (not shown) _{that stores NaHCO 3 in a slurry or solid state, and stores Ca(OH) 2} Ca (OH) ₂ a storage tank 146 and, NH ₄ Cl and Ca (OH) is reacted by the following [Chemical formula 5] by an agitator 147, a ₂ NH ₃ regeneration tank for reproducing NH ₃ (148 to ).

Here, the NaCl silo 141 can supply NaCl solid powder to the mixing tank 143 by a screw 141a rotated by a motor, and to prevent the NaCl solid powder from agglomeration due to moisture in the air. Dry air can be periodically and uniformly sprayed into the NaCl silo 141.

On the other hand, when NaCl is supplied as a saturated aqueous solution, the concentration of aqueous ammonia including water is diluted and the _{cost of regeneration of NH 3} is increased, so that unlike using a saturated NaCl aqueous solution or seawater directly using NaCl solid powder, additional water is added. There is no need for this, there is no reduction in the concentration of ammonia water, the size of the device at the rear end of the membrane filter 144 can be reduced, and the consumption amount of Ca(OH) _{2 used for NH 3 regeneration can be reduced.}

In addition, the membrane filter 144 sucks the solution and sediment from the mixing tank 143 and separates NaHCO ₃ and other by-product sediment by transferring the sediment at high pressure by the high pressure pump 145.

Further, NH ₃ in the regeneration tank NH ₃ for ammonia production unit 120 is stored in (148) NH ₃ injection nozzles (123b) and the NO _X absorbent 131 claim 1 NH ₃ was supplied to the spray nozzle (131b) re-use of By doing so, it is possible to save cost by reducing _{relatively expensive NH 3 , and an aqueous solution containing CaCl 2} (aq) as a reactant and remaining NaCl or NH4Cl is discharged outboard.

Next, as shown in FIG. 7, the steam generating unit 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 has changed phase, and a supply pump 154 and a control valve that control and supply the amount of boiler water from the cascade tank 153 to the auxiliary boiler 151 Consisting of (155), it generates and supplies steam necessary for heating equipment on board the ship.

Here, when the load of the ship 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 8, 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 including 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 adjustment, 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 can be stored and stored separately.

On the other hand, NaOH may be exemplified as a neutralizing agent for meeting the conditions for outboard discharge, but it is assumed that the substances discharged from the absorption tower 130 are both acidic or basic, so that these acids or basics can be neutralized, respectively, if 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 are separated and discharged from the exhaust gas to meet IMO GHG emission regulations, and _{CO 2} is removed after removing _{SO X.} Removal of CO ₂ solubility and CO ₂ removal efficiency can be improved, NH ₃ regeneration cost can be reduced by using NaCl solid powder, the size of the device at the rear end of the membrane filter can be reduced, and when CO _{2 is} removed, NH ₃ and Ca(OH) ) _{It is possible to reduce the removal cost because only 2} is consumed, NaHCO3 with little impurities can be stored as a solid, and side reactions caused by SO _{X remaining during NH 3} regeneration can be removed so that impurities are not 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 111: 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
125: blower 126: pressure gauge valve
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: NaCl silo 142: stirrer
143: mixing tank 144: membrane filter
145: high pressure pump 146: Ca(OH) ₂ storage tank
147: stirrer 148: NH ₃ regeneration tank
150: steam generating unit 151: auxiliary boiler
152: boiler water circulation water pump 153: cascade tank
154: supply pump 155: control valve
160: discharge unit 161: washing water tank
162: transfer pump 163: water treatment device
164: sludge storage tank 10: ship engine

Claims (23)

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 supplying the NH 4} HCO ₃ (aq) discharged from the absorption tower by sequentially reacting with NaCl(s) and Ca(OH) _{2 to regenerate NH 3} and return to the ammonia water production unit for supply. ,
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 stacking
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
Characterized in that it comprises a; ammonia water pump for supplying the ammonia water drained to the lower end of the ammonia water production tower to the upper end of the CO _{2 removal unit,}
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 to the top 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 is,
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,
It characterized in that NH ₃ is supplied directly from the ammonia regeneration unit to the NH _{3 injection nozzle through a blower or a compressor, or when NH 3} is insufficient, _{NH 3} is supplied from a _{separate NH 3} storage tank to replace the shortfall. ,
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 replace the deficit by being supplied by 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 to the NO X absorbing part,}
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 according to any one of claims 1 to 4,
The ammonia regeneration unit,
NaCl silo for storing and supplying NaCl solid powder;
A mixing tank for generating _{NaHCO 3} (s) and NH _{4 Cl by stirring NH 4} HCO ₃ (aq) and NaCl(s) discharged from the absorption tower with a stirrer;
Membrane filter to remove the NH ₄ Cl to the suction NaHCO ₃ (s) and NH ₄ Cl from the mixing tank;
A high pressure pump for transferring a mixture of NaHCO ₃ (s) and NH _{4 Cl to the membrane filter at high pressure;
NaHCO 3} storage tank for storing _{NaHCO 3} in a slurry or solid state;
Ca (OH) Ca (OH) 2 storage tank for storing the _two; And
It characterized in that it comprises; _{NH 3} regeneration tank for regenerating _{NH 3 by reacting NH 4} Cl and Ca(OH) ₂ by a stirrer,
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, including 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.

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