Flue gas adjustment

Abstract

The gas conditioning system removes contaminants, including nitrogen oxides and sulfur oxides, from the ship's flue gas and includes an oxidizer unit and a direct contact cooler. The oxidizer unit receives exhaust flue gas from the marine engine via a fluid inlet at a temperature of 150°C to 550°C and converts at least some of the nitrogen oxides in the flue gas into nitrogen gas, nitrogen dioxide, or both. The direct contact cooler is fluidly connected to the oxidizer unit and includes a housing that defines a cooling chamber. The direct contact cooler cools the flue gas to a temperature of 60°C or less by bringing it into contact with seawater present in the cooling chamber. The seawater removes some or all of the nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber.

Description

[Technical Field]

[0001] Cross-reference of related applications This application claims priority to U.S. Patent Application No. 63 / 508,370, filed on 15 June 2023. The disclosures of the prior application are deemed to be part of the disclosures of this application, and the entirety thereof is incorporated into this application. This disclosure relates to gas control systems, such as those for adjusting flue gases. [Background technology]

[0002] Fuel supply engines, such as marine diesel engines, produce exhaust gases containing various pollutants. In marine diesel engines, these pollutants include nitrogen oxides, sulfur oxides, and carbon dioxide. U.S. and international regulations aim to limit the concentrations of certain pollutants that may be emitted by marine diesel engines. [Overview of the project]

[0003] This disclosure describes gas regulation systems, such as flue gas regulation systems for flue gases from ships.

[0004] In some embodiments, a gas conditioning system for removing contaminants, including nitrogen oxides and sulfur oxides, from a ship's flue gas includes an oxidizer unit including a first fluid inlet and a first fluid outlet, the oxidizer unit receiving exhaust flue gas from a marine engine through the first fluid inlet at a temperature of 150°C to 550°C. The oxidizer unit converts at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C. The gas conditioning system also includes a direct contact cooler comprising a second fluid inlet fluid-connected to the first fluid outlet of the oxidizer unit, a housing defining a cooling chamber, and a second fluid outlet. The direct contact cooler cools the flue gas to a temperature of 60°C or less by bringing it into contact with seawater present in the cooling chamber. The seawater removes nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber.

[0005] These and other embodiments may include one or more of the following features: The oxidizer unit can receive exhaust flue gas from a marine engine via a first fluid inlet at a temperature of 150°C to 350°C, and the oxidizer unit can convert at least a portion of nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C. The direct contact cooler can cool the flue gas to a temperature of 50°C or less. The oxidizer unit can receive exhaust flue gas from a marine engine via a first fluid inlet at a temperature of 150°C to 310°C, and the oxidizer unit can convert at least a portion of nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 310°C. The oxidizer unit can convert at least a portion of sulfur oxides in the flue gas to sulfur dioxide at a temperature of 150°C to 550°C, and the direct contact cooler can separate nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber. The oxidizer unit may include a housing defining an oxidation chamber and an oxidizer present within the oxidation chamber and in direct contact with the exhaust flue gas. The oxidizer may include a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite, which comes into contact with the flue gas and converts at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide. The oxidizer unit may include a selective catalytic reduction unit for converting a portion of the nitrogen oxides into at least one of nitrogen gas or nitrogen dioxide at temperatures between 150°C and 550°C. The gas conditioning system may further include an adsorption unit including a third fluid inlet fluid-connected to a second fluid outlet of a direct contact cooler, the adsorption unit receiving flue gas from the direct contact cooler and removing at least a portion of residual nitrogen oxides from the flue gas from the direct contact cooler. The adsorption unit may include at least one adsorption bed, and the gas conditioning system may guide the flue gas from the third fluid inlet through at least one adsorption bed, the adsorption bed capable of reducing the nitrogen oxide content from the flue gas to less than 50 ppm. The adsorption bed can reduce the nitrogen oxide content from flue gas to less than 10 ppm. The adsorption unit can include two adsorption beds.A selective catalytic reduction unit may include a second housing defining a second chamber and a compound inlet for introducing a mist of a compound solution into the second chamber, and a first fluid inlet may guide flue gas into contact with the compound solution in the second chamber. The compound solution may include urea or ammonia. The selective catalytic reduction unit may include a catalyst located in the second chamber, which comes into contact with the flue gas and the mist of the compound solution. The gas conditioning system may further include a filter located upstream of the first fluid inlet, which removes particulate matter and volatile hydrocarbons from the flue gas. The filter may be directly coupled to the oxidizer unit at the first fluid inlet of the oxidizer unit. The gas conditioning system may further include a blower unit located between the marine engine and the first fluid inlet of the oxidizer unit, which guides the flue gas to the oxidizer unit and increases the pressure of the flue gas. The gas conditioning system may further include a blower unit positioned downstream of the direct contact cooler, which generates a partial vacuum in the flue gas flow path through the oxidizer and direct contact cooler, thereby facilitating the flow of flue gas through the oxidizer and direct contact cooler toward the blower unit. The direct contact cooler may include a rotating packed bed comprising a housing surrounding a cooling chamber, a rotor drum positioned within the housing and rotatable about a pivot axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing, and a second fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet. The flue gas may be positioned in a countercurrent flow relative to the seawater in the rotor drum when the rotating packed bed is in use. The direct contact cooler may include a seawater inlet for introducing seawater into the cooling chamber, which removes at least some of the sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The gas conditioning system may further include a water treatment system that is fluidly connected to a direct contact cooler and receives seawater from the direct contact cooler, the water treatment system including a membrane and an input system for adjusting the pH of the seawater to be greater than 6.5.The gas conditioning system may further include a rotary packed bed assembly that is fluidly connected to a direct contact cooler and receives flue gas from the direct contact cooler, the rotary packed bed assembly may include a first rotary packed bed having an absorbent that absorbs at least a portion of carbon dioxide from the flue gas, and a second rotary packed bed that receives the absorbent from the first rotary packed bed and desorbs the carbon dioxide absorbed from the absorbent. The absorbent may include a liquid solvent. The liquid solvent may include an amine solvent. The rotary packed bed assembly may include a water washing station that is fluidly connected to the first rotary packed bed, the water washing station washing the flue gas from the first rotary packed bed with water. The water washing station may include a filling cylinder or a rotary packed bed. The gas conditioning system may further include a storage system that is fluidly connected to the second rotary packed bed and includes a compressor and a storage tank, the storage system receiving the desorbed carbon dioxide, compressing the desorbed carbon dioxide with the compressor, and storing the carbon dioxide in the storage tank.

[0006] Certain aspects of the present disclosure encompass a method for adjusting flue gas from a ship. The method includes the steps of: receiving exhaust flue gas from a marine engine at a temperature of 150°C to 550°C in a chamber of an oxidizer unit; using reactants in the chamber of the oxidizer unit to convert a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C; receiving the flue gas from the oxidizer unit in a direct contact cooler; and cooling the flue gas to a temperature of 60°C or less by bringing the flue gas into direct contact with seawater in the direct contact cooler.

[0007] These and other embodiments may include one or more of the following features: The exhaust flue gas may be received from a marine engine at a temperature of 150°C to 350°C, and some of the nitrogen oxides may be converted at a temperature of 150°C to 350°C. The conversion using reactants in the chamber of the oxidizer unit may further include converting some of the sulfur oxides in the flue gas to sulfur dioxide, and cooling the flue gas with seawater may include removing at least some of the sulfur dioxide and nitrogen dioxide from the flue gas with seawater in response to direct contact between the flue gas and seawater. The oxidizer unit may include a selective catalytic reduction unit, and the conversion may include converting some of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C. The reactants may include a catalyst, and the conversion of a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide may include guiding the flue gas to contact a mist of a compound solution in a chamber, and further guiding the flue gas and the mist of the compound solution toward a catalyst in the chamber. The compound solution may include a urea solution or an ammonia solution. The method may further include receiving cooled flue gas from a direct contact cooler in an adsorption unit, and removing at least a portion of the remaining nitrogen oxides from the cooled flue gas in the adsorption unit. Removing at least a portion of the remaining nitrogen oxides from the cooled flue gas may include guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm, for example, less than 10 ppm. The method may further include increasing the pressure of the flue gas using a blower unit positioned between the marine engine and the oxidizer unit, and guiding the flue gas to the oxidizer unit using the blower unit.The method may further include the steps of generating a partial vacuum in the flow path of flue gas through an oxidizer unit and a direct contact cooler using a blower unit located downstream of a direct contact cooler, and guiding the flue gas through the oxidizer unit and the blower unit toward the blower unit using the blower unit. The method may further include filtering particulate matter and volatile hydrocarbons from the flue gas with a filter located upstream of the oxidizer unit. The direct contact cooler may include a rotating packed bed, and cooling the flue gas may include guiding the flue gas in the rotating packed bed into a countercurrent flow relative to the seawater in the rotating packed bed. Guiding the flue gas in the rotating packed bed into a countercurrent flow relative to the seawater in the rotating packed bed may include transferring at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas to the seawater. The method may further include guiding the flue gas from the direct contact cooler to a first rotating packed bed containing an absorbent, and absorbing at least a portion of the carbon dioxide from the flue gas using the absorbent in the first rotating packed bed. The method may further include the steps of introducing an absorbent containing absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed. The method may further include the steps of introducing the desorbed carbon dioxide to a storage system, compressing the carbon dioxide in a compressor in the storage system, and storing the compressed carbon dioxide in a storage tank in the storage system. The method may further include introducing flue gas from a first rotating packed bed to a water washing station including a housing surrounding a washing chamber, and washing the flue gas with water in the washing chamber of the water washing station. Receiving exhaust flue gas from a marine engine may include receiving the exhaust flue gas at a temperature of 250°C or less, and converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide may include converting at a flue gas temperature of 250°C or less.

[0008] Some aspects of this disclosure encompass gas conditioning systems for removing contaminants, including nitrogen oxides and sulfur oxides, from the flue gas of a ship. The gas conditioning system includes an oxidizer unit having a first fluid inlet and a first fluid outlet, which receives exhaust flue gas through the first fluid inlet and converts at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide; and a direct contact cooler having a rotating packed bed for bringing the flue gas into contact with seawater and cooling the flue gas to a temperature of 60°C or less. The seawater is for removing nitrogen dioxide and sulfur dioxide from the flue gas. The rotating packed bed includes a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing and the first fluid outlet of the oxidizer unit, and a second fluid outlet fluid-connected to the rotor drum. Flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet.

[0009] This and other embodiments may include one or more of the following features: The flue gas may be arranged in a countercurrent flow relative to the seawater in the rotor drum when the rotating packed bed is in use. A seawater inlet introduces seawater into the rotor drum, and the seawater removes at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The oxidizer unit may include a selective catalytic reduction unit, which receives exhaust flue gas at a temperature of 150°C to 350°C and can convert a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C. The selective catalytic reduction unit may include a second housing defining a second chamber and a compound inlet for introducing a mist of compound solution into the second chamber, with a first fluid inlet leading the flue gas to contact the mist of compound solution in the second chamber. The compound solution may include urea or ammonia. A selective catalytic reduction unit may be located in a second chamber and may include a catalyst that comes into contact with the flue gas and a mist of the compound solution in the second chamber. The gas conditioning system may further include an adsorption unit having a third fluid inlet fluidly connected to a second fluid outlet of a direct contact cooler, the adsorption unit receiving flue gas from the direct contact cooler and removing at least a portion of residual nitrogen oxides from the flue gas from the direct contact cooler. The adsorption unit may include at least one adsorption bed, and the gas conditioning system guides the flue gas from the third fluid inlet through at least one adsorption bed, the adsorption bed reducing the nitrogen oxide content from the flue gas to less than 10 ppm. The adsorption unit may include two adsorption beds. The gas conditioning system may further include a filter located upstream of the first fluid inlet, the filter removing particulate matter and volatile hydrocarbons from the flue gas. The filter may be directly coupled to the oxidizer unit at the first fluid inlet of the oxidizer unit. The gas regulation system may further include a blower unit located upstream of the first fluid inlet of the oxidizer unit, which directs flue gas to the oxidizer unit and increases the pressure of the flue gas.The gas conditioning system may further include a blower unit located downstream of the direct contact cooler, which generates a partial vacuum in the flow path of flue gas through the oxidizer unit and the direct contact cooler, thereby facilitating the flow of flue gas through the oxidizer and the direct contact cooler toward the blower unit. The gas conditioning system may further include a rotary packed bed assembly fluidly connected to the direct contact cooler and receiving flue gas from the direct contact cooler, which includes a first rotary packed bed having an absorbent that absorbs at least a portion of carbon dioxide from the flue gas, and a second rotary packed bed that receives the absorbent from the first rotary packed bed and desorbs the carbon dioxide absorbed from the absorbent. The rotary packed bed assembly may further include a water washing station fluidly connected to the first rotary packed bed, which washes the flue gas from the first rotary packed bed with water. The water washing station may include a filling cylinder or a rotary packed bed. The gas adjustment system is fluidly connected to a second rotating packed bed and may further include a storage system comprising a compressor and a storage tank, the storage system receiving the desorbed carbon dioxide, compressing the desorbed carbon dioxide with the compressor, and storing the carbon dioxide in the storage tank.

[0010] Certain aspects of the present disclosure encompass a method for preparing flue gas. The method includes the steps of: receiving exhaust flue gas in a chamber of an oxidizer unit; converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide with reactants in the chamber of the oxidizer unit; receiving the flue gas from the oxidizer unit in a direct contact cooler, wherein the direct contact cooler includes a rotating packed bed; and cooling the flue gas in the rotating packed bed to a temperature of 60°C or less by bringing it into contact with seawater in the rotating packed bed.

[0011] These and other embodiments may include one or more of the following features: Conversion using reactants in the chamber of the oxidizer unit may further include converting a portion of sulfur oxides in the flue gas to sulfur dioxide; contacting the flue gas in the rotating packed bed with seawater in the rotating packed bed may include transferring at least a portion of sulfur dioxide and nitrogen dioxide in the flue gas to seawater; the directing step may include directing the flue gas into a countercurrent flow relative to the seawater in the rotating packed bed; the oxidizer unit may include a selective catalytic reduction unit, receiving the exhaust flue gas may include receiving the exhaust flue gas in the chamber of the selective catalytic reduction unit at a temperature of 150°C to 550°C; and conversion of a portion of nitrogen oxides may include converting a portion of nitrogen oxides to nitrogen gas at a temperature of 150°C to 550°C, or 150°C to 350°C. The reactants may include a catalyst, and the conversion of a portion of nitrogen oxides into nitrogen gas may include guiding the flue gas into contact with a mist of a compound solution in a chamber, and further guiding the flue gas and the mist of the compound solution toward the catalyst in the chamber. The compound solution may include a urea solution or an ammonia solution. The method may further include receiving cooled flue gas from a direct contact cooler in an adsorption unit, and removing at least a portion of the remaining nitrogen oxides from the cooled flue gas in the adsorption unit. Removing at least a portion of the remaining nitrogen oxides from the cooled flue gas may include guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content from the flue gas to less than 50 ppm or less than 10 ppm. The method may further include increasing the pressure of the flue gas in a blower unit located upstream of the oxidizer unit, and guiding the flue gas to the oxidizer unit in the blower unit.The method may further include the steps of: generating a partial vacuum in the flow path of flue gas through the oxidizer unit and the direct contact cooler using a blower unit located downstream of the direct contact cooler; and guiding the flue gas through the oxidizer unit and the blower unit toward the blower unit using the blower unit. The method may further include filtering particulate matter and volatile hydrocarbons from the flue gas with a filter located upstream of the oxidizer unit. The method may further include the steps of: guiding the flue gas from the direct contact cooler to a first rotating packed bed having an absorbent; and absorbing at least a portion of the carbon dioxide from the flue gas using the absorbent in the first rotating packed bed. The method may further include the steps of: guiding the absorbent having absorbed carbon dioxide to a second rotating packed bed; and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed. The method may further include the steps of: guiding the desorbed carbon dioxide to a storage system; compressing the carbon dioxide with a compressor in the storage system; and storing the compressed carbon dioxide in a storage tank in the storage system. The method may further include the steps of: guiding flue gas from a first rotating packed bed to a water washing station having a housing surrounding a washing chamber; and washing the flue gas with water in the washing chamber of the water washing station.

[0012] In some embodiments, a gas conditioning system for removing contaminants, including nitrogen oxides and sulfur oxides, from a ship's flue gas includes a contactor, a direct contact cooler, and an adsorption unit. The contactor includes a contactor housing defining a first chamber and an oxidizer present in the first chamber, the contactor receiving exhaust flue gas from a marine engine in the first chamber and contacting the flue gas with the oxidizer to convert at least some of the nitrogen oxides in the flue gas into nitrogen dioxide. The direct contact cooler receives exhaust flue gas from the contactor and includes a rotating packed bed for contacting the flue gas with seawater to cool the flue gas to a temperature of 60°C or less. The seawater removes nitrogen dioxide and sulfur dioxide from the flue gas. The rotating packed bed includes a housing surrounding the cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a first fluid inlet fluid-connected to the housing, and a first fluid outlet fluid-connected to the rotor drum. Flue gas is introduced from a first fluid inlet to a first fluid outlet, and seawater is introduced from a seawater inlet to a seawater outlet. The adsorption unit includes a second fluid inlet fluid-connected to the first fluid outlet of the direct contact cooler, and a filled cylinder. The adsorption unit receives flue gas from the direct contact cooler and removes at least a portion of the remaining nitrogen oxides from the flue gas, reducing the nitrogen oxide content of the flue gas to less than 10 ppm.

[0013] These and other embodiments may include one or more of the following features: The flue gas may be arranged in a countercurrent flow to the seawater in the rotor drum when the rotating packed bed is in use. A seawater inlet may guide seawater into the rotor drum, and the seawater removes at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The adsorption unit may include at least one adsorption bed, which guides the flue gas through at least one adsorption bed. The oxidizing agent may include a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite. The gas conditioning system may further include a rotating packed bed assembly that is fluidly connected to the adsorption unit and receives the flue gas from the adsorption unit, the rotating packed bed assembly including a first rotating packed bed having an absorbent that absorbs at least a portion of carbon dioxide from the flue gas, and a second rotating packed bed that receives the absorbent from the first rotating packed bed and desorbs the carbon dioxide absorbed from the absorbent. The rotary packed bed assembly may further include a water washing station fluid-connected to a first rotary packed bed, the water washing station washing flue gas from the first rotary packed bed with water. The water washing station may include a filling cylinder or a rotary packed bed. The gas conditioning system may further include a storage system fluid-connected to a second rotary packed bed, the storage system receiving desorbed carbon dioxide, compressing the desorbed carbon dioxide with the compressor, and storing the carbon dioxide in the storage tank.

[0014] Certain aspects of the present disclosure encompass a method for regulating flue gas from a ship. The method includes the steps of receiving exhaust flue gas from a marine engine into a first chamber of a contactor, wherein the contactor includes a contactor housing defining the first chamber and an oxidizer present in the first chamber, and guiding the flue gas into contact with the oxidizer in the first chamber of the contactor in order to convert at least a portion of the nitrogen oxides in the flue gas into nitrogen dioxide. The method further includes receiving exhaust flue gas from the contactor in a direct contact cooler, wherein the direct contact cooler includes a rotating packed bed, and guiding the flue gas in the rotating packed bed into contact with seawater in the rotating packed bed to cool the flue gas to a temperature of 60°C or less.

[0015] These and other embodiments may include one or more of the following features. The method may further include the steps of receiving cooled flue gas from a direct contact cooler in an adsorption unit, and removing the remainder of nitrogen oxides from the flue gas in a packed cylinder of the adsorption unit. Removing the remainder of nitrogen oxides from the flue gas may include guiding the flue gas through at least one adsorption bed of the packed cylinder to reduce the nitrogen oxide content from the flue gas to less than 10 ppm. Guiding the flue gas to contact seawater may include guiding the flue gas into a countercurrent flow relative to the seawater in the rotating packed bed. Guiding the flue gas in the rotating packed bed to seawater in the rotating packed bed may include transferring at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas to the seawater. Contacting the flue gas with an oxidizer in the first chamber of the contactor may include contacting the flue gas with a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite present in the first chamber to convert at least some of the nitrogen oxides in the flue gas into nitrogen dioxide. The method may further include increasing the pressure of the flue gas using a blower unit positioned between the marine engine and the contactor, and directing the flue gas towards the contactor using the blower unit. The method may further include filtering and removing particulate matter and volatile hydrocarbons from the flue gas using a filter positioned upstream of the contactor. The method may further include leading the flue gas to a first rotating packed bed having an absorbent, and absorbing at least some of the carbon dioxide from the flue gas using the absorbent in the first rotating packed bed. The method may further include leading the absorbent having the absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed. This method may further include the steps of: introducing the desorbed carbon dioxide into a storage system; compressing the carbon dioxide using a compressor in the storage system; and storing the compressed carbon dioxide in a storage tank in the storage system.The method may further include the steps of: directing flue gas from a first rotating packed bed to a water washing station including a housing surrounding a washing chamber; and washing the flue gas with water in the washing chamber of the water washing station.

[0016] Some aspects of the present disclosure describe a gas conditioning system for removing pollutants, including carbon dioxide, from flue gas. The gas conditioning system includes a rotary packed bed assembly fluidly connected to the exhaust port of an engine, the rotary packed bed assembly receiving flue gas from the exhaust port. The rotary packed bed assembly includes a first rotary packed bed having an absorbent that absorbs a portion of the carbon dioxide from the flue gas, and a second rotary packed bed that receives the absorbent from the first rotary packed bed and desorbs at least a portion of the carbon dioxide from the absorbent.

[0017] These and other embodiments may include one or more of the following features: The absorbent may include a liquid solvent. The liquid solvent may include an amine solvent. The rotary packed bed assembly may further include a water washing station fluid-connected to the first rotary packed bed, the water washing station washing flue gas from the first rotary packed bed with water. The water washing station may include a packing cylinder or a rotary packed bed. The rotary packed bed assembly may further include a third rotary packed bed in series with the first rotary packed bed, the third rotary packed bed containing a second portion of the absorbent, and the third rotary packed bed absorbing a second portion of carbon dioxide from the flue gas. The rotary packed bed assembly may further include an intercooler fluid-connected to the first and third rotary packed beds, the intercooler cooling a second portion of the absorbent and guiding the second portion of the absorbent to the first rotary packed bed. The rotary packed bed assembly may further include an intercooler fluid-coupled to a first rotary packed bed and a third rotary packed bed, the intercooler cooling a first portion of the absorbent and directing the first portion of the absorbent to the third rotary packed bed. The rotary packed bed assembly may further include a third rotary packed bed parallel to the first rotary packed bed, the first rotary packed bed receiving a first portion of flue gas, the third rotary packed bed receiving a second portion of flue gas, and the third rotary packed bed containing a second portion of the absorbent. The rotary packed bed assembly may further include a fourth rotary packed bed in series with the second rotary packed bed, the fourth rotary packed bed receiving the absorbent from the second rotary packed bed and desorbing at least a portion of the carbon dioxide from the absorbent. The rotary packed bed assembly may further include an interheater fluid-coupled to the second and fourth rotary packed beds, the interheater heating the absorbent from the second rotary packed bed and directing the absorbent to the fourth rotary packed bed. The rotary filling bed assembly may further include a fourth rotary filling bed parallel to a second rotary filling bed, the second rotary filling bed receiving a first portion of the absorbent and the fourth rotary filling bed receiving a second portion of the absorbent.The gas adjustment system is fluidly connected to a second rotating packed bed and may further include a storage system including a compressor and a storage tank, the storage system receiving desorbed carbon dioxide, compressing the desorbed carbon dioxide with the compressor, and storing the carbon dioxide in the storage tank. The gas adjustment system may further include a selective catalytic reduction unit fluidly positioned upstream of the rotating packed bed assembly between the exhaust port and the rotating packed bed assembly, the selective catalytic reduction unit including a fluid inlet and a fluid outlet fluidly connected to the exhaust port, the selective catalytic reduction unit receiving flue gas from the exhaust port through the fluid inlet and converting at least a portion of the nitrogen oxides in the flue gas into nitrogen gas. The selective catalytic reduction unit can receive exhaust flue gas from the engine at a temperature of 150°C to 550°C and convert a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C. The selective catalytic reduction unit may include a housing defining a chamber and a compound inlet for introducing a mist of compound solution into the chamber, the fluid inlet leading the flue gas into contact with the mist of compound solution in the chamber. The compound solution may include urea or ammonia. The selective catalytic reduction unit may include a catalyst placed in a chamber, which comes into contact with the flue gas and a mist of the urea solution in the chamber. The gas conditioning system may further include an oxidizer unit having a fluid inlet fluidly connected to the exhaust flue gas from the engine and a fluid outlet fluidly connected to a rotating packed bed assembly, the oxidizer unit receiving the exhaust flue gas from the engine through the fluid inlet and converting at least a portion of the nitrogen oxides in the flue gas to nitrogen dioxide and at least a portion of the sulfur dioxide in the flue gas to sulfur dioxide. The gas conditioning system may further include a direct contact cooler located upstream of the rotating packed bed assembly and fluidly positioned between the exhaust port and the rotating packed bed assembly, the direct contact cooler including a fluid inlet fluidly connected to the exhaust port, a housing surrounding a cooling chamber, and a fluid outlet, the direct contact cooler directing the flue gas into contact with seawater present in the cooling chamber and cooling the flue gas to a temperature of 60°C or less.The direct contact cooler may include a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, and a third rotating packed bed having a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a fluid inlet fluid-connected to the housing, and a fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the fluid inlet to the fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet. The flue gas may be arranged in a countercurrent flow with respect to the seawater in the rotor drum when the third rotating packed bed is in use. The direct contact cooler may include a seawater inlet for introducing seawater into the cooling chamber, and the seawater removes at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The gas conditioning system may further include an adsorption unit located upstream of the rotating packed bed assembly and fluidly positioned between the exhaust port and the rotating packed bed assembly, the adsorption unit having a fluid inlet fluid-connected to the exhaust port, the adsorption unit receiving flue gas from the exhaust port and removing at least a portion of nitrogen oxides from the flue gas. The adsorption unit may include at least one adsorption bed, and the gas conditioning system guides flue gas from the fluid inlet through at least one adsorption bed, which reduces the nitrogen oxide content from the flue gas to less than 10 ppm.

[0018] Specific examples of the present disclosure include a method for regulating flue gas. The method includes the steps of introducing flue gas from an exhaust port into a rotating bed assembly, wherein the rotating bed assembly includes a first rotating bed and a second rotating bed, and absorbing at least a portion of carbon dioxide from the flue gas using an absorbent in the first rotating bed. The method also includes the steps of introducing the absorbent having absorbed carbon dioxide from the first rotating bed to the second rotating bed, and desorbing carbon dioxide from the absorbent in the second rotating bed.

[0019] These and other embodiments may include one or more of the following features: The method may further include the steps of introducing desorbed carbon dioxide into a storage system, compressing the carbon dioxide using a compressor in the storage system, and storing the compressed carbon dioxide using a storage tank in the storage system. The method may further include introducing flue gas from a first rotating bed to a water washing station, and washing the flue gas with water in a washing chamber of the water washing station. The rotating bed assembly may further include a third rotating bed in series with the first rotating bed and containing a second portion of absorbent, and the method may further include introducing flue gas from the first rotating bed to the third rotating bed, and absorbing the second portion of carbon dioxide from the flue gas with the second portion of absorbent in the third rotating bed. The method may further include the steps of: introducing a second portion of the absorbent from a third rotating packed bed to an intercooler fluid-coupled to the first and third rotating packed beds; cooling the second portion of the absorbent in the intercooler; and introducing the cooled second portion of the absorbent to the first rotating packed bed. The method may further include the steps of: introducing a first portion of the absorbent from a first rotating packed bed to an intercooler fluid-coupled to the first and third rotating packed beds; cooling the first portion of the absorbent in the intercooler; and introducing the cooled first portion of the absorbent to the third rotating packed bed. The rotating packed bed assembly may further include a fourth rotating packed bed in series with the second rotating packed bed, and the method may further include introducing the absorbent from the second rotating packed bed to the fourth rotating packed bed; and desorbing at least a portion of the carbon dioxide from the absorbent in the fourth rotating packed bed. Guiding the absorbent from the second rotating packed bed to the fourth rotating packed bed may include guiding the absorbent from the second rotating packed bed to an interheater fluidly coupled to the second and fourth rotating packed beds, heating the absorbent in the interheater, and guiding the heated absorbent to the fourth rotating packed bed.The method may further include the steps of: receiving flue gas from an exhaust port at a temperature of 150°C to 550°C in a chamber of an oxidizer unit fluidly positioned between an exhaust port and a rotating packed bed assembly; and converting a portion of nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C using a reactant in the chamber of the oxidizer unit. The reactant may include an oxidizing agent, and the conversion using the reactant in the chamber of the oxidizer unit may further include converting a portion of sulfur oxides in the flue gas to sulfur dioxide using the oxidizing agent. The oxidizer unit may include a selective catalytic reduction unit, and the conversion may include converting a portion of nitrogen oxides in the flue gas to nitrogen gas at a temperature of 150°C to 550°C. The reactant may include a catalyst, and the conversion of a portion of nitrogen oxides in the flue gas to nitrogen gas may include guiding the flue gas to contact a mist of a compound solution in the chamber, and further guiding the flue gas and the mist of the compound solution toward the catalyst in the chamber. The compound solution may include a urea solution or an ammonia solution. The method may further include the steps of receiving flue gas from the exhaust port in a direct contact cooler fluidly positioned between the exhaust port and the rotating packed bed assembly, and cooling the flue gas to a temperature of 60°C or less by bringing the flue gas into direct contact with seawater within the direct contact cooler. The method may further include the steps of receiving flue gas from the direct contact cooler in an adsorption unit, and removing at least a portion of the remaining nitrogen oxides from the cooled flue gas in the adsorption unit. Removing at least a portion of the remaining nitrogen oxides from the cooled flue gas may include guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm.

[0020] Details of one or more embodiments of the subject matter described herein are given in the accompanying drawings and the following description. Other features, aspects, and advantages of the subject matter will become apparent from the description, drawings, and claims.

Brief Description of the Drawings

[0021] [Figure 1] It is a schematic block flow diagram of an exemplary adjustment system for adjusting flue gas from a marine engine. [Figure 2] It is an exemplary schematic perspective view of an exemplary rotary packed bed system that can be used in the exemplary adjustment system of FIG. 1. [Figure 3] It is a perspective view of an exemplary ship including a gas adjustment system attached to an exemplary ship. [Figure 4] It is a flowchart illustrating an exemplary method for adjusting flue gas from a ship. [Figure 5] It is a flowchart illustrating another exemplary method for adjusting flue gas. [Figure 6] It is a flowchart illustrating another exemplary method for adjusting flue gas from a ship. [Figure 7] It is a flowchart illustrating another exemplary method for adjusting adhesive gas.

Best Mode for Carrying Out the Invention

[0022] Like reference numerals in the various drawings indicate like elements.

[0023] This disclosure describes a gas adjustment system for treating and adjusting flue gas, such as flue gas from a marine engine, to remove or reduce pollutant emissions from the flue gas. Pollutants include carbon dioxide (CO2), nitrogen oxides (i.e., nitrogen dioxide (NO2), nitric oxide (NO), dinitrogen monoxide (N2O), or a combination of N2O, NO2, and / or NO including x )), sulfur oxides (i.e., sulfur dioxide (SO2), sulfur monoxide (SO), or SO including both SO2 and SO x), particulate matter, volatile hydrocarbons, combinations thereof, or other contaminants may be included. Vessels may include container ships, tankers, vehicle carriers, cruise liners, or other vessels that include one or more marine engines. In some examples, gas regulating systems may be retrofitted to existing vessels and positioned to block the flow of flue gas between the exhaust outlets of the marine engines and the exhaust stack outlets of the vessel.

[0024] Contaminants from flue gases of marine diesel engines may contain higher concentrations of sulfur oxides, nitrogen oxides, or both compared to the sulfur oxide and nitrogen oxide concentrations of other land-based engine systems. The solvent used to separate contaminants from the gas flow may vary depending on the type of contaminant to be separated. In some embodiments, the gas conditioning system pre-conditions the flue gas to remove all or part of sulfur oxides, nitrogen oxides, or all or part of both sulfur oxides and nitrogen oxides before removing all or part of CO2 from the gas. For example, sulfur oxides and / or nitrogen oxides may overwhelm, decompose, or otherwise adversely affect the solvent used for CO2 removal from the flue gas, resulting in insufficient or incomplete CO2 removal. Pre-treatment of the flue gas removes or reduces sulfur oxides and / or nitrogen oxides before CO2 treatment, allowing for more efficient removal of contaminants from the flue gas while efficiently utilizing the solvent. In certain embodiments of pre-conditioning the flue gas in a gas conditioning system, seawater is used to cool the flue gas in contact with it or to remove NO from the flue gas. x and SO x The seawater can be recycled, and / or treated before recycling by passing it through a wastewater system (i.e., a water treatment system), either in whole or in part.

[0025] Marine vessels operate under U.S. and / or international emission regulations, such as those of the International Maritime Organization (IMO) 2020 under Annex VI of MARPOL. Under these emission regulations, pollutants in flue gas must be below certain threshold values ​​for CO2 and other pollutants. Some of these regulations have led the industry to pursue cleaner, more expensive fuels as they result in lower concentrations of pollutants in flue gas. However, the gas conditioning systems of this disclosure can be implemented on vessels to better condition flue gas from marine engines and remove higher concentrations and more pollutants from flue gas, even when processing flue gas from engines that consume fuels with higher concentrations of sulfur.

[0026] In certain onshore flue gas treatment systems, packed columns are used to treat carbon emissions from flue gas. However, packed columns require a large spatial footprint and may not function properly on moving platforms (e.g., not on a stationary ground-mounted platform). In gas conditioning systems of this disclosure, such as gas conditioning systems on ships, the use of large-footprint devices (such as packed columns) is reduced or avoided in order to efficiently maximize limited space while maintaining sufficient operational performance. For example, a gas conditioning system may include one or more rotating packed beds (RPBs) at various stages of conditioning operations, such as direct contact cooling, CO2 absorption, CO2 desorption, rinsing, or other operational stages typically performed by larger-footprint devices such as packed columns in onshore systems. Packed columns on moving platforms, such as platforms on operating ships, may perform poorly due to poor solvent distribution caused by the moving ship. The effect of movement on the liquid / gas distribution within the column affects column performance for at least two reasons. The first reason is the static tilt of the column from the vertical. The amplitude and / or period of vibration (e.g., tilt) can divert the liquid within the column from its axial path, which is normally expected in onshore absorption or regeneration columns. The strain resulting from non-perpendicularity can cause liquid accumulation in some parts of the column, drought in others, and slippage of untreated gas. A second reason is that the accelerating force generated by the movement of the ship's hull is amplified in some places by the large distance between the upper floor of the column and the center of rotation of the column. The radial force applied by acceleration can cause the liquid to deviate from a uniform distribution within the column. This uneven distribution can affect contact between the liquid and gas phases, reducing the effective area for mass transfer between the phases.The gas regulating system of this disclosure offers advantages including reduced spatial footprint, the ability to process various contaminants from flue gas (i.e., nitrogen oxides, sulfur oxides, CO2, and / or other contaminants), regulating operation that can be performed on a mobile platform (such as a mobile vessel), improved contaminant capture capability, increased operational flexibility (such as high turndown capability), and / or reduced energy consumption required to carry out contaminant capture from the flue gas flow.

[0027] This disclosure describes a gas conditioning system for use in ships and for regulating flue gases from marine engines of ships. However, the gas conditioning systems described herein can be used in other engine systems for processing other types of flue gases, such as onshore engine systems. For example, the gas conditioning systems described herein can be connected to the exhaust systems of marine diesel engines on ships, furnaces in manufacturing facilities, refineries, cement plants, steel mills or factories, mobile onshore generators, combinations thereof, or other onshore hydrocarbon combustion sources.

[0028] Figure 1 is a schematic block flow diagram of an exemplary gas conditioning system 100 for conditioning flue gas from an engine such as a marine diesel engine of a ship. The exemplary conditioning system 100 can be implemented on a ship, but it can also be implemented on a different engine system separate from a ship. The exemplary gas conditioning system 100 receives the flue gas flow from the engine, removes contaminants from the flue gas, and releases the conditioned flue gas after the removal or reduction of contaminants. The exemplary gas conditioning system 100 includes a carbon dioxide capture system 102 for separating carbon dioxide from the flue gas flowing through the carbon dioxide capture system 102, a pre-conditioning system 200 for pre-treatment of the flue gas before it flows into the carbon dioxide system 102, and a storage system 104 for storing the carbon dioxide separated from the flue gas in the carbon dioxide system 102.

[0029] During the operation of the exemplary gas conditioning system 100, flue gas from the engine flows through the pre-conditioning system 200 to reduce or remove certain contaminants from the flue gas, such as nitrogen oxides and sulfur oxides. For example, flue gas from the engine's exhaust stack 110 is directed to the pre-conditioning system 200. In some examples, a blower 112 directs flue gas from the exhaust stack 110 (or other exhaust components from the engine) to the pre-conditioning system 200. The blower 112 increases or maintains the pressure of the flue gas to overcome any final pressure drop in the flue gas as it flows through the pre-conditioning system 200 and / or carbon dioxide capture system 102, preventing back pressure in the ship's engine. Although the blower 112 is shown in Figure 1 as being between the exhaust stack 110 and the pre-conditioning system 200, the location of the blower 112 can be changed. For example, the blower 112 can be located between components or inside the pre-conditioning system 200 itself, such as downstream of components of the pre-conditioning system 200. In some embodiments, the blower 112 is positioned downstream of the direct contact cooler (described later) of the pre-conditioning system 200 to create a partial vacuum in the exhaust gas flow through the components of the pre-conditioning system 200 upstream of the blower 112. The partial vacuum provides a draft flow of exhaust gas toward the blower 112 through the upstream components (i.e., between the exhaust stack 110 and the blower 112). At the blower 112, the pressure of the exhaust gas is increased in preparation for flowing toward downstream components such as the carbon dioxide capture system 102. The blower 112 or additional blowers can be positioned at other locations along the exhaust gas flow to create a partial vacuum in the exhaust gas flow, increase the pressure of the exhaust gas, or both.

[0030] In the pre-conditioning system 200, once nitrogen oxides and / or sulfur oxides are removed from the flue gas, or the concentrations of nitrogen oxides and sulfur oxides in the flue gas are reduced to below the maximum threshold concentration, the resulting flue gas flows to the carbon dioxide capture system 102, where carbon dioxide is removed from the flue gas, or the concentration of carbon dioxide is reduced to below an acceptable threshold. The resulting clean flue gas from the carbon dioxide capture system 102 is released into the atmosphere, and the removed carbon dioxide is led to the storage system 104. The storage system 104 accepts and stores carbon dioxide, for example, during the navigation of a ship.

[0031] In an exemplary gas conditioning system 100, a carbon dioxide capture system 102 receives flue gas from a pre-conditioning system 200 and removes all or part of the carbon dioxide from the flue gas. In some examples, the flue gas flow can bypass the pre-conditioning system 200 and flow directly to the carbon dioxide capture system 102 from a blower 112, engine exhaust outlet, or other engine exhaust component. The carbon dioxide capture system 102 includes a rotating packed bed assembly that is fluidly connected to the engine exhaust port and receives the flue gas. An exemplary RPB system is shown in Figure 2 and described later. The rotating packed bed assembly includes a first rotating packed bed 120 called an RPB absorber 120, which contains an absorbent for absorbing some of the carbon dioxide from the flue gas. Absorbents are substances used to capture contaminants (such as carbon dioxide) from a fluid flow (e.g., a flue gas flow) by chemisorption (e.g., amine solutions, sodium hydroxide, aqueous ammonia, carbonic anhydrase, combinations thereof, and / or other substances), physical absorption (e.g., methanol, glycol, dimethyl ether, combinations thereof, or other substances), or by a mixture of chemisorbents or physical absorbents. Absorbents can vary, for example, based on the type of contaminant that is to be absorbed or adsorbed from the flue gas. In some examples, the absorbent contains a solvent, such as a liquid solvent and / or chemical solvent, for absorbing carbon dioxide (or other contaminants). For example, the liquid solvent may include amine solvents, amino acids, sodium hydroxide (NaOH), potassium hydroxide (KOH), potassium carbonate (K2CO3), ionic liquids, inorganic solvents, combinations thereof, or other solvents. In the exemplary gas control system 100 in Figure 1, the absorbent contains an amine solvent, however, other absorbents can be used to absorb carbon dioxide and / or other contaminants from the flue gas.

[0032] The rotary bed assembly also includes a second rotary bed 122, called an RPB desorber, which receives an absorbent from the first rotary bed 120 and desorbs at least a portion of the carbon dioxide from the absorbent.

[0033] The RPB absorber 120 absorbs carbon dioxide from the flue gas and binds the carbon dioxide to an absorbent. For example, flue gas enters the RPB absorber 120, comes into contact with the absorbent, where CO2 enters the liquid phase and reacts with the absorbent. After absorption, the treated flue gas can exit the RPB absorber 120 and be released into the atmosphere. In some embodiments, such as the exemplary gas conditioning system 100 in Figure 1, the rotating packed bed assembly of the carbon dioxide capture system 102 also includes a water washing station 124 fluidly connected to the first rotating packed bed 120. The water washing station 124 washes the flue gas from the first rotating packed bed 120 with water to remove any residual volatile absorbent that may be exiting the RPB absorber 120 along with the purified flue gas. The water washing station 124 can take various forms, such as a packed cylinder or a rotating packed bed, in which the water in the water washing station 124 comes into contact with the flue gas from the RPB absorber 120. The water in which the absorbent has been captured can be returned to the RPB absorber 120, for example, to be recombined with the absorbent for reuse or recycling.

[0034] In some embodiments, the RPB absorber 120 may include multiple RPBs arranged in series, in parallel, or in a combination of parallel and series RPBs. In an exemplary system, the RPB absorber 120 includes two series RPBs, forming a first and second RPB absorber, and the flue gas travels through the series-arranged first and second RPB absorbers. The first RPB absorber may include a first portion of absorbent for absorbing a first portion of carbon dioxide in the flue gas, and the second RPB absorber may include a second portion of absorbent for absorbing a second portion of carbon dioxide in the flue gas. One or both of the first or second RPB absorbers may be fluidly connected to a water flushing station 124 for flushing the flue gas. In examples with multiple RPB absorbers, the water flushing station 124 may be connected to the last RPB absorber in the exemplary RPB assembly (e.g., the furthest downstream absorber RPB). In certain embodiments, the rotating packed bed assembly also includes a fluid-coupled intercooler between the RPB absorbers. The intercooler can be used to cool the absorbent, such as a first or second portion of the absorbent, and to guide the cooled absorbent to the first or second RPB absorber. In certain cases where the RPB absorber 120 includes multiple RPBs, the intercooler can be positioned between one, more, or all pairs of series RPBs. The temperature rise of the flue gas / liquid agent may occur due to higher absorption heat and lower heat capacity, which shifts the equilibrium in the chamber. One or more intercoolers can control the temperature rise to approach isothermal conditions, for example. The effectiveness of intercooling depends at least in part on the properties of the absorbent, such as absorption heat and physical properties, as well as the ratio of gas flow rate to liquid flow rate through the RPBs.

[0035] The number and arrangement of RPBs in the RPB absorber 120 can vary, for example, to include multiple RPBs in series, multiple RPBs in parallel, or arrangements of RPBs including both series and parallel RPBs. For example, parallel RPBs can be used to process large amounts of flue gas at once, series RPBs can be used to better cool the absorbent, promote more complete saturation of the absorbent, capture contaminants more effectively and efficiently, reduce the amount of absorbent used, or a combination of these. The arrangement of RPBs in the RPB absorber 120 can include series RPBs, parallel RPBs, or a combination thereof to optimize flue gas conditioning. In some embodiments, the RPB absorber 120 can include multiple RPBs including parallel and series arrangements, and a flow controller (not shown) can guide the flue gas through one or more paths along the arrangement to optimize the characteristics of the flue gas. For example, the flow controller can direct the flue gas to two (or more) parallel RPBs when the flow of flue gas to the RPB absorber 120 increases, and / or the flow controller can direct the flue gas to two (or more) series RPBs when more complete absorption of contaminants by the absorbent is desired.

[0036] In the RPB desorber 122, the rich absorbent received from the RPB absorber 120 flows through the RPB desorber 122 and comes into contact with steam from the reboiler 126. The rich absorbent is heated to break the bonds between CO2 and the absorbent, and the CO2 is removed from the absorbent in contact with the steam. In some examples, after stripping the CO2 from the absorbent, the absorbent can be returned to the RPB absorber 120 for reuse or recycled in another way. The CO2 captured from the RPB desorber 122 can be led to a storage system 104, which will be described later.

[0037] In some embodiments, the RPB desorber 122 may include multiple RPBs arranged in series, parallel, or in combination of parallel and series RPBs. In an exemplary system, the RPB desorber 122 includes two series RPBs, forming a first RPB desorber and a second RPB desorber, and the absorbent moves through the series-arranged first and second RPB desorbers. The first RPB desorber can remove (or desorb) a first portion of CO2 from the absorbent, and the subsequent second RPB desorber can remove a second portion of CO2 from the absorbent. In certain embodiments, the rotating bed assembly also includes an interheater fluidly coupled to the first and second RPB desorbers, such as between the RPB desorbers. The interheater can be used to heat the absorbent as it moves from the first RPB desorber to the second RPB desorber. In certain cases where the RPB detacher 122 includes multiple RPBs, the interheater can be placed between one, more, or all pairs of series RPBs.

[0038] The number and arrangement of RPBs in the RPB desorber 122 may vary, for example, to include multiple RPBs in series, multiple RPBs in parallel, or arrangements of RPBs including both series and parallel RPBs. For example, parallel RPBs can be used to process large amounts of rich absorbent at once, series RPBs can be used to increase the heating of the absorbent, promote more complete regeneration of the absorbent, desorb contaminants from the absorbent more effectively and efficiently, reduce the amount of steam required in the reboiler 126, or a combination thereof. The arrangement of RPBs in the RPB desorber 122 may include series RPBs, parallel RPBs, or a combination thereof to optimize absorbent desorption and adjustment. In some implementations, the RPB desorber 122 may include multiple RPBs including parallel and series arrangements, and a flow controller (not shown) may guide the absorbent (e.g., liquid amine solvent or other liquid solvent) through one or more paths along the arrangement to optimize the properties of the absorbent. For example, the flow controller may direct the absorbent to two (or more) parallel RPBs if the flow of absorbent to the RPB desorber 122 is increased, and / or the flow controller may direct the absorbent to two (or more) series RPBs if more complete desorption of contaminants from the absorbent is desired. In some embodiments of the RPB system incorporating one or more intercoolers and one or more interheaters, the properties of the absorbent (e.g., liquid amine solvent) and its optimal configuration may help to obtain an optimal ratio between the partial pressure of water and CO2, thereby reducing the overall energy consumption during absorbent regeneration.

[0039] The carbon dioxide capture system 102 of the exemplary gas conditioning system 100 includes an RPB for initiating interaction between two fluids, such as between flue gas and absorbent in the case of an RPB absorber, or between absorbent and vapor in the case of an RPB desorber. In a particular embodiment in which the exemplary gas conditioning system 100 is deployed on a ship, the use of an RPB ensures fluid interaction and liquid distribution between the two fluids, even while the ship is moving at sea. Conversely, a column relies on gravity-driven motion for fluid interaction, and if it relies on gravity-driven motion on a moving platform, it can result in liquid misdistribution caused by the movement of the moving platform (e.g., ship movement). Instead, an RPB operates with little to no performance degradation based on the uneven distribution of absorbent caused by platform movement, while reducing the overall footprint required for the fluid interaction unit compared to, for example, a column.

[0040] In some embodiments, the carbon dioxide capture system 102 of the exemplary gas conditioning system 100 may include additional components to optimize the flow rate, flow composition, temperature, pressure, or other properties of the flue gas, absorbent, and / or captured contaminants (e.g., carbon dioxide). For example, the carbon dioxide capture system 102 includes a first exchanger 128 located between the RPB absorber 120 and the RPB desorber 122, and a second exchanger 130 located between the RPB desorber 122 and the storage system 104. The first exchanger 128 is a heat exchanger that transfers heat between the rich absorbent (e.g., rich amine solvent) flowing from the RPB absorber 120 to the RPB desorber 122 and the lean absorbent (e.g., dilute amine solvent) flowing from the RPB desorber 122 to the RPB absorber 120. In some cases, the first exchanger 128 transfers heat from the dilute absorbent to the rich absorbent to lower the temperature of the dilute amine solvent and raise the temperature of the rich amine solvent. The first heat exchanger 128 may include a plate and flame heat exchanger or other types of cross-exchanger. The second exchanger 130 is a cross-exchanger, gas-liquid separator, or both, which receives a mixture of water and carbon dioxide from the RPB desorber 122 and separates carbon dioxide from the water. The second exchanger 130 separates carbon dioxide from the water-CO2 mixture from the RPB desorber 122, for example, to remove water from the mixture before leading the CO2 to the storage system 104. In some examples, the second exchanger 130 includes a flash separator drum that receives a stream of water and a stream of the carbon dioxide and water mixture from the RPB desorber 122 and outputs a stream of water and a separate stream of separated carbon dioxide. The separated carbon dioxide flow into the storage system 104, and the water flow from the second exchanger 130 can be discharged or recycled in an internal or external system of the exemplary gas adjustment system 100.

[0041] The storage system 104 of the exemplary gas conditioning system 100 is fluidly connected to a downstream unit of the carbon dioxide capture system 102 (e.g., a second rotating packed bed 122) and receives the captured CO2, and optionally, water and trace impurities evaporated with the captured CO2. The storage system 104 cools the CO2 to remove water, compresses the CO2, and cools it further to liquefy and store the CO2. The storage system 104 includes a compressor 106, a refrigeration system 107, and a storage tank 108. The refrigeration system 107 cools the captured CO2, the compressor 106 compresses the captured CO2 to a pressure of 320 pounds / square inch absolute (psia) or more, and the storage tank 108 stores the CO2 once it reaches its liquid phase. The storage system 104 can operate to store the captured CO2 at a range of temperatures and pressures. For example, the storage system 104 can store captured CO2 within a temperature range of -56.6°C (-69.88°F) to 31°C (87.8°F) and / or a pressure range of 5.2 bar to less than 74 bar (75.42 to 1073.28 psia).

[0042] An exemplary gas conditioning system 100 preconditioning system 200 is located upstream of the carbon dioxide capture system 102 along the flue gas flow from the engine and preconditions the flue gas before it flows into the carbon dioxide capture system 102. The preconditioning system 200 conditions the flue gas to remove some or all sulfur oxides, some or all nitrogen oxides, particulate matter, volatile hydrocarbons, combinations thereof, or other contaminants from the flue gas. In some examples, removing nitrogen oxides and sulfur oxides from the flue gas before the carbon dioxide capture system 102 allows the absorbent in the carbon dioxide capture system 102 to remove CO2 more effectively from the flue gas. Otherwise, the presence of nitrogen oxides, sulfur oxides, or both in the flue gas adversely affects the performance of the absorbent and reduces the lifespan of the absorbent in the carbon dioxide capture system 102. The exemplary gas conditioning system 100 preconditioning system 200 includes a filter 202, an oxidizer 204, a direct contact cooler 206, and a polisher 208. The filter 202, oxidizer 204, direct contact cooler 206, and polisher 208 are arranged in series with respect to each other so that the flue gas flows through the filter 202, then the oxidizer 204, then the direct contact cooler 206, and then the polisher 208. However, the order of these devices may differ, and one or more of these devices may be completely excluded from the pre-conditioning system 200. For example, the pre-conditioning system 200 may exclude the filter 202, the oxidizer 204, the direct contact cooler 206, the polisher 208, or any combination of these components. In a particular example, the pre-conditioning system 200 includes a flow control device (e.g., a fluid valve) and a flow path for guiding the flue gas through the pre-conditioning system 200 along a desired flow path. The flow control device and / or flow path can guide flue gas through one, more, or all components of the pre-conditioning system 200, and can be operated so that flue gas can bypass one, more, or all components of the pre-conditioning system 200 between the engine and the carbon dioxide capture system 102.

[0043] The filter 202 removes or reduces particulate matter, volatile hydrocarbons, or both from the flue gas. The filter 202 may include a housing having a filter medium. The filter is located upstream of the oxidizer 204 and the direct contact cooler 206 and filters the flue gas before it flows into the oxidizer 204 and / or the direct contact cooler 206. In some embodiments, the filter 202 may be coupled to, attached to, or integrated with the oxidizer 204, for example, by being located within the fluid inlet of the oxidizer 204 into which the flue gas is led.

[0044] The oxidizer 204, direct contact cooler 206, polisher 208, or a combination of these features may include a packed bed, a packed cylinder, or a combination of these structures for guiding the flue gas into contact with the material. A packed bed is a container that can be filled (partially or completely) with a material intended to contact and / or interact with a fluid flowing through the packed bed. The material may form a support structure and may be coated with a catalyst. The catalyst can be varied, such as NO x , SO x or may be selective for the reduction of other contaminants. The packed bed can have various heights and shapes. A packed cylinder is a container placed within the internal space of a vessel and filled (partially or completely) with a porous packing material. The porosity, shape, and / or arrangement of the packing material provide an effective contact area between fluids, such as between a liquid phase and a vapor phase. The packing material includes one or more packing material units arranged as a cartridge structure within the vessel, which can increase effective mass transfer between the fluids in contact and reduce the pressure drop of the fluid flowing through the packed cylinder. In some embodiments, the packed cylinder is smaller in size than the packed column and can operate with a forced flow of fluid through the cylinder (i.e., as previously stated, the packed cylinder is not gravity-driven as the packed column operates).

[0045] The oxidizer 204 is a vessel or device that directs contact between the inlet fluid and reactants to facilitate a chemical reaction within the inlet fluid. The reactants may include oxidizing agents such as oxygen, ozone, hydrogen peroxide, sodium hypochlorite, sodium chlorite (NaClO2), or other oxidizing agents. The oxidizer 204 may include a packed bed or packed cartridge to direct contact between the inlet fluid and the oxidizing agent. Contact between the inlet fluid and the oxidizing agent facilitates the conversion of one or more components of the inlet fluid to water-soluble species. In the exemplary pre-conditioning system 200 of Figure 1, the oxidizer 204 brings the flue gas into contact with the oxidizer, for example, to convert some or all of the NO in the flue gas to the more water-soluble NO2 species. The oxidizer 204 includes a fluid inlet and a fluid outlet, and an oxidizer housing that defines the oxidation chamber. The oxidizer 204 receives the exhaust flue gas through the fluid inlet, oxidizes all or part of the flue gas in the oxidation chamber, and leads the flue gas out through the fluid outlet. The oxidizer 204 converts all or part of the nitrogen oxides (NO) present in the flue gas in the oxidizer 204 (e.g., within the oxidation chamber) into nitrogen gas (N2) or nitrogen dioxide (NO2), or both. In some embodiments, the oxidizer 204 also converts all or part of the sulfur oxides (SO) present in the flue gas of the oxidizer 204 into sulfur dioxide (SO2). N2, NO2, and SO2 are more easily separated from the flue gas than NO and SO, as will be described in more detail later.

[0046] The oxidizer 204 can support an oxidizing agent as a solid, liquid, or gas, and the oxidizing agent is supported within a chamber and brought into contact with the flue gas flowing through the chamber. In some examples, the oxidizing agent is in liquid form, such as a solution of the oxidizing agent, and is introduced into the flue gas in cross-flow, counter-flow, or co-flow with the flue gas. In some embodiments, the oxidizer 204 includes a contactor 220 integrated with the oxidizer 204, such as within the chamber of the oxidizer 204. The contactor 220 introduces sodium chlorite or other oxidizing agent into the flue gas flowing through the contactor 220. In some examples, the oxidizing agent is sodium chlorite, introduced into the contactor as a solution of NaClO2, and comes into direct contact with the flue gas in counter-flow or cross-flow, etc. The contactor 220 includes a housing that defines a chamber (e.g., a separate chamber of the oxidizer 204 or the same chamber), and the sodium chlorite is either present in the chamber or introduced into the chamber in liquid form via one or more nozzles or other fluid pathways. Flue gas is introduced into the chamber to come into contact with sodium chlorite. Upon contact with the flue gas, the sodium chlorite oxidizes some or all of the nitrogen oxides (NO) in the flue gas to nitrogen dioxide (NO2), thereby reducing the nitrogen oxide (NO) content. In some embodiments, a direct contact cooler 206 receives the flue gas from the contactor 220 and removes some or all of the nitrogen dioxide from the flue gas. In certain embodiments, an adsorption unit 218 (described later) receives the flue gas flow from the direct contact cooler 206 and removes some or all of any remaining nitrogen oxides (NO, NO2, or both) from the flue gas before directing the flue gas flow to the carbon dioxide removal system 102.

[0047] The oxidizer 204 can receive flue gas at a range of temperatures and can still function to convert nitrogen oxides and / or sulfur oxides in the flue gas to nitrogen dioxide and / or sulfur dioxide. For example, the oxidizer 204 can receive flue gas at a low temperature of 150°C, such as 150°C to 550°C, 150°C to 350°C, or 150°C to 310°C, and can convert NO and / or SO present in the flue gas at that temperature (e.g., 150°C to 550°C, 350°C, or 310°C) to NO2 and / or SO2. In some embodiments, the pre-conditioning system 200 includes a heater 210 upstream of the oxidizer unit 204 to heat the flue gas to a desired temperature. In certain cases, the flue gas can bypass the heater and flow directly to the oxidizer 204 without being heated by the heater 210.

[0048] In some cases, flue gas can exit the engine at a temperature of approximately 250°C and either pass through a waste heat boiler to lower the temperature of the flue gas, or pass through a heater (e.g., heater 210) or boiler to raise the temperature of the flue gas, or flow directly to a pre-conditioning system 200. In conventional combustion waste gas treatment systems, the temperature of the flue gas exiting the engine typically reaches or exceeds approximately 350°C (e.g., land-based engines) or is heated to or above approximately 350°C (e.g., marine-based engines). Heating the flue gas to high temperatures such as above 350°C allows for easier oxidation of contaminants in the flue gas to more readily remove the same contaminants. However, raising the temperature of the flue gas may require additional energy and a separate heating unit. In the exemplary gas conditioning system 100 shown in Figure 1, the oxidizer 204 receives flue gas at a temperature below 350°C, such as 150°C to 310°C, and can oxidize selected contaminants from the flue gas without the additional energy consumption and / or heating unit that would normally be required when heating the flue gas to 310°C or above (e.g., 350°C or above).

[0049] In some embodiments, the oxidizer 204 includes a selective catalytic reduction (SCR) unit, the reactant is a catalyst, and the SCR unit uses the catalyst to convert some of the nitrogen oxides (NO x ) to nitrogen gas (N2). The SCR unit is a container or device such as a packed bed that guides contact between the inlet fluid and the catalyst, and the contact between the inlet fluid and the catalyst promotes the conversion of one or more oxide gas components of the inlet fluid to a gas and water-based version. For example, in the exemplary preconditioning system 200 of FIG. 1, the SCR unit contacts the flue gas with the catalyst and uses the catalyst to convert some or all of the NO x in the flue gas to nitrogen gas (N2) and water (H2O) to assist the reaction. The catalyst can vary. The SCR unit includes a chamber and a compound inlet 212 for introducing a solution of the compound into the chamber. The compound can be various. For example, the compound can include urea, ammonia, or other compounds that promote the conversion of nitrogen oxides to nitrogen gas. In some cases, the compound inlet 212 introduces the compound solution as a mist (e.g., a mist of urea, a mist of ammonia, or both), and the flue gas contacts the mist of the compound solution. The SCR unit also includes a catalyst present in the chamber to interact with the flue gas and compound mist mixture and induces a chemical reaction to convert nitrogen oxides to nitrogen gas. The following equations 1 and 2 define the chemical reactions that occur between the flue gas and the urea solution on the catalyst. 3NO + CO(NH2)2 → (5 / 2)N2 + 2H2O + CO2 Equation 1 3NO2 + 2CO(NH2)2 → (7 / 2)N2 + 4H2O + CO2 Equation 2 The following equations 3 and 4 define the chemical reactions that occur between the flue gas and the ammonia solution on the catalyst. 4NO + 4NH3 + O2 → 4N2 + 6H2O Equation 3 6NO2 + 8NH3 → 7N2 + 12H2O Equation 4 Nitrogen gas is not considered a pollutant and is effectively inert in flue gas. Nitrogen oxides (NO xConverting contaminants into nitrogen gas, water, and carbon dioxide effectively reduces the concentration of nitrogen-based contaminants in the flue gas or eliminates their presence. The catalyst can vary. In some embodiments, the catalyst includes a porous medium, such as a honeycomb structure of material, placed in a chamber to interact with the flue gas and compound solution mixture. However, the catalyst can take other forms, shapes, and materials. For example, the catalyst may include a packed bed of porous medium, and the catalyst material may include coated aluminum, ceramic material, or other material. In some examples, the porous medium provides a desired pressure drop for the fluid flowing through the catalyst.

[0050] A direct contact cooler 206 is a container or device that cools an inlet fluid by bringing it into direct contact with a cooler fluid. The direct contact cooler 206 may include a packed bed or packed cartridge to direct contact between the inlet fluid and a relatively cooler fluid. The contact between the inlet fluid and the cooler fluid may be counterflow, parallel flow, crossflow, or another relative flow direction. The direct contact cooler 206 of an exemplary gas conditioning system 100 includes a fluid inlet, a fluid outlet, and a cooling chamber defined by the housing of the direct contact cooler 206. The fluid inlet may be directly connected to the fluid outlet of the oxidizer 204, to a filter 202, to a blower 112, or to an engine exhaust component to receive the flue gas flow. The direct contact cooler 206 cools the flue gas to a desired temperature by bringing it into contact with seawater present in the cooling chamber, such as seawater entering through a seawater inlet 214. The desired temperature can vary, such as being below 60°C or below 50°C, for example, 40°C.

[0051] In a ship, the direct contact cooler 206 has access to abundant seawater, and the temperature of the seawater (e.g., below 32°C) is lower than the temperature of the flue gas entering the direct contact cooler 206. When the seawater comes into contact with the flue gas, it cools the flue gas to a lower temperature, such as 60°C, 50°C, 40°C, or another temperature lower than 60°C or 50°C. In addition to cooling the flue gas, the seawater can remove nitrogen dioxide, sulfur dioxide, or both nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber. The seawater has a basic pH (e.g., a pH between 8.0 and 8.2), and in some cases, the solubility of NO2 and / or SO2 in water allows the seawater to remove SO2 and / or NO2 from the flue gas without other catalysts or solvents.

[0052] Removing NO2 and / or SO2 from flue gases with seawater can lower the pH of the seawater. In some embodiments, the pre-conditioning system 200 includes a water treatment system 216 that receives seawater for use in the direct contact cooler 206 and treats the seawater to adjust its pH, turbidity, polycyclic aromatic hydrocarbon (PAH) content, and / or nitrate content. The water treatment system 216 treats the seawater to enable discharge of used seawater overboard, but still complies with regulatory requirements for seawater disposal or recycling. The water treatment system 216 of an exemplary gas conditioning system 100 includes a housing defining an internal chamber, a membrane (e.g., a ceramic membrane) placed within the internal chamber, and an injection system (using NaOH or another buffer solution) for adjusting the pH of the seawater to exceed the permissible limit for overboard disposal (e.g., pH above 6.5). During operation, seawater is introduced into the internal chamber and comes into contact with the membrane, and the injection system supplies the conditioning solution to the internal chamber. The injection system may include an injection pump for supplying a controlled amount of the conditioning solution to the discharged seawater. The water treatment system 216 may also include temperature sensors for monitoring the seawater temperature to ensure that the seawater temperature is maintained below a maximum threshold temperature, such as 60°C as established by IMO 2020.

[0053] In some embodiments, the direct contact cooler 206 includes a rotating packed bed (RPB) that guides the flue gas into contact with seawater. Figure 2 is a schematic perspective view of an exemplary rotating packed bed system 250 that can be used in the exemplary gas conditioning system 100 of Figure 1, including a direct contact cooler 206 for guiding the flue gas into a countercurrent flow relative to seawater. The exemplary RPB system 250 includes a housing 252 surrounding a chamber 254 and a rotor drum 256 located within the housing 252 and rotatable about a rotation axis AA. In some embodiments, the exemplary RPB system 250 includes a motor 258 connected to the rotor drum 256 by a drive shaft or the like (e.g., directly or indirectly coupled) to drive the rotation of the rotor drum 256 about the rotation axis AA. The rotor drum 256 defines a radial flow path through the body of the rotor drum 256 between the radial outer surface of the drum and the interior of the rotor drum 256. In some cases, the radial flow path includes individual radial channels through the body of the rotor drum, extending from an opening on the outer surface of the rotor drum to the internal space of the rotor drum close to its radial center (i.e., near the axis of rotation AA). The radial flow path can define an array of paths that fluidly connect the open space in the chamber 254 to the interior of the rotor drum 256. In certain embodiments, the rotor drum 256 may contain a filler material, which can define radial flow paths through the rotor drum 256. The filler material can facilitate contact and mass transfer between the liquid and gas flowing through the exemplary RPB system 250.

[0054] An exemplary RPB system 250 includes a fluid inlet 260 fluid-connected to the interior of the rotor drum 256, a fluid outlet 262 fluid-connected to the chamber 254 on the inner surface of the housing 252, a gas inlet 264 fluid-connected to the chamber 254 on the inner surface of the housing 252, and a gas outlet 266 fluid-connected to the interior of the rotor drum 256. During operation of the RPB system 250, liquid flows into the interior of the rotor drum 256 through the liquid inlet 260, and the rotation of the rotor drum 256 directs the liquid flow through the radial passage of the rotor drum 256 radially outward relative to the axis of rotation AA. As the liquid flows out from the outer surface of the rotor drum 256, the liquid subsequently flows toward the liquid outlet 262 on the inner wall of the housing 252. Conversely, gas flows into the chamber 254 through the gas inlet 264, flows toward the interior of the rotor drum 256 into the radial passage of the rotor drum 256, and subsequently flows toward the gas outlet 266. In the exemplary RPB system 250 shown in Figure 2, the gas and liquid are arranged to flow in opposite directions within the radial flow path of the rotor drum 256, such that the liquid flow flows in the opposite direction to the gas flow. For example, the liquid flows radially outward through the rotor drum 256 relative to the rotation axis AA, and the gas flows radially inward through the rotor drum 256 relative to the rotation axis AA, and the gas and liquid contact in counterflow when they flow opposite each other. In some embodiments, the liquid flows radially outward through the rotor drum in response to the centrifugal force from the rotation of the rotor drum 256, which provides a high surface area for mass transfer between the gas and liquid when the counterflowing gas contacts the droplets toward the outer radial surface of the rotor drum 256.

[0055] In the exemplary RPB system 250 shown in Figure 2, the rotor drum 256 is oriented so that its rotation axis AA is horizontal. However, this configuration and orientation can vary. For example, the rotor drum 256 can be oriented to rotate around an axis that is horizontal, vertical, or an intermediate angle between vertical and horizontal.

[0056] Referring again to the direct contact cooler 206 of the exemplary gas conditioning system 100 in Figure 1, the direct contact cooler 206 may include an RPB, as in the exemplary RPB system 250 in Figure 2. For example, the direct contact cooler 206 may include a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a pivot axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing, and a second fluid outlet fluid-connected to the rotor drum. In exemplary operation, flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet, and when a rotating packed bed is used (e.g., the rotor drum is rotating), the flue gas is arranged in a countercurrent flow relative to the seawater in the rotor drum. During operation, seawater is guided into the cooling chamber, and the seawater can remove at least a portion of sulfur dioxide, nitrogen dioxide, or both from the flue gas in the cooling chamber. In some cases, flue gas can be flowed in parallel with seawater.

[0057] Polisher 208 is a container or device that removes trace amounts of contaminants from a fluid by reaction or adsorption using a porous medium. Polisher 208 may include a filled bed or filled cartridge to direct contact between the fluid and the material. For example, in the exemplary pre-conditioning system 200 of Figure 1, Polisher 208 removes SO4 from the flue gas before it enters the carbon dioxide capture system 102. x and / or NO xTo remove any remaining traces, the flue gas is brought into contact with the particles on the support structure within the cylinder of the polisher 208. The polisher 208 in an exemplary pre-conditioning system 200 includes a filling cylinder, a fluid inlet fluid-connected to the fluid outlet of a direct-contact cooler 206, and an adsorption unit 218 including the fluid outlet. The adsorption unit 218 receives the flue gas from the direct-contact cooler 206 and removes all or part of the remaining nitrogen oxides (e.g., NO, NO2, or both) from the flue gas. In some embodiments, the flue gas flow bypasses the polisher 208 or the polisher 208 is completely removed, for example, when the flue gas has a nitrogen oxide (NO) concentration below a maximum threshold concentration. For example, if an oxidizer 204 converts all (all or substantially) of the nitrogen oxides (NO) in the flue gas to nitrogen dioxide (NO2), and then the direct-contact cooler 206 removes nitrogen dioxide from the flue gas, the polisher 208 can be bypassed or excluded from the pre-conditioning system 200. However, if the oxidizer 204 converts only a portion of the NO to NO2, and the concentration of NO in the flue gas after the oxidizer 204 and direct contact cooler 206 exceeds the maximum threshold concentration, the flue gas flow is directed to the polisher 208, and the adsorption unit 218 can remove some or all of the remaining NO from the flue gas before it flows to the carbon dioxide removal system 102. x In certain cases, such as when including an SCR unit that provides (which leaves NO in the flue gas), Polisher 208 is used to remove the remaining NO from the flue gas. x Some or all of it can be removed. However, the SCR unit converts nitrogen oxides in the flue gas into nitrogen gas, and NO in the flue gas. x If the remaining amount is zero or otherwise below the maximum threshold concentration, the flue gas can bypass the polisher 208, or the polisher 208 can be completely excluded from the pre-conditioning system 200.

[0058] The adsorption unit 218 can take various forms. In some examples, the adsorption unit includes one or more adsorption beds (e.g., one, two, or more adsorption beds), and the flue gas is guided through one or more adsorption beds. Each adsorption bed can reduce the nitrogen oxide content from the flue gas to below a threshold nitrogen concentration, such as 50 ppm or less, 10 ppm or less, or another concentration less than 50 ppm. In examples where the adsorption unit includes two or more adsorption beds, one adsorption bed is used at a time, the first adsorption bed is saturated with flue gas, and the other adsorption beds are regenerated, for example, by applying heat and scavenging airflow to the other adsorption beds.

[0059] Some components or all of the exemplary gas conditioning system 100 can be housed in a single housing, such as in a container or housing type, for modular positioning of the gas conditioning system 100. The housing can be mounted on a ship, located in a factory, or located near an engine's exhaust system and fluidly connected to the exhaust system, in order to handle the gas flowing through the exemplary gas conditioning system 100. For example, Figure 3 is a perspective view of an exemplary ship 300 including a gas conditioning system 302 mounted on the deck of the exemplary ship 300. The exemplary ship 300 includes a marine engine (not shown) and an exhaust system 304, and the gas conditioning system 302 is connected to the exhaust system 304 and regulates the flue gas to, for example, remove contaminants by shutting off the flue gas through the exhaust system 304. The gas adjustment system 302 may be the same as the exemplary gas adjustment system 100 in Figure 1, but may also be installed inside a vessel and on the exemplary vessel 300.

[0060] Figure 3 shows an exemplary gas regulation system 302 installed on a ship, but the gas regulation system 302 can be used in different exhaust systems and / or other technological spaces other than ships.

[0061] Figure 4 is a flowchart illustrating an exemplary method 400 for adjusting flue gas. The exemplary method 400 can be performed by the exemplary gas adjustment system 100 in Figure 1 and can be used to adjust flue gas from a vessel such as the exemplary vessel 300 in Figure 3. In 402, exhaust flue gas from a marine engine is received in the chamber of an oxidizer unit at a temperature of 150°C to 350°C. In 404, some of the nitrogen oxides in the flue gas are converted to nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C using reactants in the chamber of the oxidizer unit. In 406, the flue gas is received from the oxidizer unit in a direct contact cooler. In 408, the flue gas is cooled to a temperature of 50°C or less by bringing the flue gas into direct contact with seawater in the direct contact cooler.

[0062] Figure 5 is a flowchart illustrating another exemplary method 500 for adjusting flue gas. The exemplary method 500 can be performed by the exemplary gas adjustment system 100 of Figure 1 and can be used to adjust flue gas from a vessel such as the exemplary vessel 300 of Figure 3. In 502, exhaust flue gas is received in the chamber of an oxidizer unit. In 504, some of the nitrogen oxides in the flue gas are converted to nitrogen gas or nitrogen dioxide using reactants in the chamber of the oxidizer unit. In 506, the flue gas from the oxidizer unit is received in a direct contact cooler. The direct contact cooler comprises a rotating packed bed. In 508, the flue gas in the rotating packed bed is guided in a countercurrent flow relative to the seawater in the rotating packed bed, cooling the flue gas to a temperature of 50°C or less.

[0063] Figure 6 is a flowchart illustrating another exemplary method 600 for adjusting flue gas from a ship. Exemplary method 600 can be performed by the exemplary gas adjustment system 100 of Figure 1 and can be used to adjust flue gas from a ship such as the exemplary ship 300 of Figure 3. In 602, exhaust flue gas from a marine engine is received into a first chamber of a contactor. The contactor comprises a contactor housing defining the first chamber and an oxidizer present in the first chamber. In 604, the flue gas is guided into contact with the oxidizer in the first chamber of the contactor, converting at least some of the nitrogen oxides in the flue gas into nitrogen dioxide. In 606, the exhaust flue gas from the contactor is received in a direct contact cooler. The direct contact cooler comprises a rotating packed bed. In 608, the flue gas in the rotating packed bed is brought into contact with seawater in the rotating packed bed to cool the flue gas to a temperature of 50°C or less.

[0064] Figure 7 is a flowchart illustrating another exemplary method 700 for adjusting adhesive gas. The exemplary method 700 can be performed by the exemplary gas adjustment system 100 of Figure 1 and can be used to adjust flue gas from a vessel such as the exemplary vessel 300 of Figure 3. In 702, flue gas is led from an exhaust port to a rotating packed bed assembly. The rotating packed bed assembly comprises a first rotating packed bed and a second rotating packed bed. In 704, at least a portion of the carbon dioxide is absorbed from the flue gas by an absorbent. In 706, the absorbent with the absorbed carbon dioxide is led from the first rotating packed bed to the second rotating packed bed. In 708, the carbon dioxide is desorbed from the absorbent in the second rotating packed bed.

[0065] In a first embodiment, a gas conditioning system for removing pollutants including nitrogen oxides and sulfur oxides from a ship's flue gas comprises: an oxidizer unit including a first fluid inlet and a first fluid outlet, configured to receive exhaust flue gas from a marine engine through the first fluid inlet at a temperature of 150°C to 550°C, and configured to convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C; and a direct contact cooler including a second fluid inlet fluidly connected to the first fluid outlet of the oxidizer unit, a housing defining a cooling chamber, and a second fluid outlet, configured to cool the flue gas to a temperature of 60°C or less by bringing it into contact with seawater present in the cooling chamber, and configured so that the seawater removes nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber.

[0066] In a second embodiment according to the first embodiment, the oxidizer unit is configured to receive exhaust flue gas from a marine engine through a first fluid inlet at a temperature of 150°C to 350°C, and the oxidizer unit is configured to convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C.

[0067] In the third embodiment according to the first or second embodiment, the direct contact cooler is configured to cool the flue gas to a temperature of 50°C or less.

[0068] In a fourth embodiment according to any of the aforementioned embodiments, the oxidizer unit is configured to receive exhaust flue gas from a marine engine through a first fluid inlet at a temperature of 150°C to 310°C, and the oxidizer unit is configured to convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 310°C.

[0069] In a fifth embodiment according to any of the aforementioned embodiments, the oxidizer unit is further configured to convert at least a portion of the sulfur oxides in the flue gas to sulfur dioxide at a temperature of 150°C to 550°C, and the direct contact cooler is configured to separate nitrogen dioxide and sulfur dioxide from the flue gas in a cooling chamber.

[0070] In a sixth embodiment according to any of the aforementioned embodiments, the oxidizer unit comprises a housing defining an oxidation chamber and an oxidizing agent present in the oxidation chamber, wherein the oxidizing agent is configured to be in direct contact with the exhaust flue gas.

[0071] In the seventh aspect according to the sixth aspect, the oxidizing agent comprises a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite, and the solution is configured to come into contact with flue gas and convert at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide.

[0072] In an eighth aspect according to any of the aforementioned embodiments, the oxidizer unit comprises a selective catalytic reduction unit configured to convert a portion of nitrogen oxides into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C.

[0073] In a ninth aspect according to the eighth aspect, the gas conditioning system further comprises an adsorption unit including a third fluid inlet fluidly connected to a second fluid outlet of a direct contact cooler, wherein the adsorption unit is configured to receive flue gas from the direct contact cooler and remove at least a portion of the remaining nitrogen oxides from the flue gas from the direct contact cooler.

[0074] In a tenth aspect according to the ninth aspect, the adsorption unit comprises at least one adsorption bed, and the gas conditioning system is configured to guide flue gas from a third fluid inlet through at least one adsorption bed, wherein the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

[0075] In the eleventh aspect according to the tenth aspect, the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

[0076] In the twelfth embodiment according to the tenth or eleventh embodiment, the adsorption unit comprises two adsorption beds.

[0077] In a thirteenth embodiment, which is one of the eighth to twelfth embodiments, the selective catalytic reduction unit comprises a second housing defining a second chamber and a compound inlet configured to introduce a mist of compound solution into the second chamber, wherein a first fluid inlet is configured to guide a flue gas into contact with the compound solution in the second chamber.

[0078] In the 14th aspect according to the 13th aspect, the compound solution contains urea or ammonia.

[0079] In the 15th embodiment according to the 13th or 14th embodiment, the selective catalytic reduction unit comprises a catalyst located in a second chamber, and the catalyst is configured to come into contact with flue gas and a mist of compound solution.

[0080] In a 16th embodiment according to any of the aforementioned embodiments, the gas conditioning system further comprises a filter located upstream of the first fluid inlet, the filter configured to remove particulate matter and volatile hydrocarbons from the flue gas.

[0081] In the 17th aspect according to the 16th aspect, the filter is directly coupled to the oxidizer unit at the first fluid inlet of the oxidizer unit.

[0082] In an 18th aspect according to any of the aforementioned embodiments, the gas conditioning system further comprises a blower unit positioned between the marine engine and a first fluid inlet of the oxidizer unit, the blower unit being configured to guide flue gas to the oxidizer unit and increase the pressure of the flue gas.

[0083] In a 19th embodiment according to any of the aforementioned embodiments, the gas conditioning system further comprises a blower unit located downstream of a direct contact cooler, the blower unit configured to generate a partial vacuum in the flow path of flue gas through the oxidizer and direct contact cooler, thereby facilitating the flow of flue gas through the oxidizer and direct contact cooler toward the blower unit.

[0084] In a 20th embodiment according to any of the aforementioned embodiments, the direct contact cooler comprises a rotating packed bed, the rotating packed bed comprising a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing, and a second fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet.

[0085] In the 21st aspect according to the 20th aspect, the flue gas is arranged in a countercurrent flow relative to the seawater in the rotor drum when the rotating packed bed is in use.

[0086] In a 22nd aspect according to any of the aforementioned embodiments, the direct contact cooler includes a seawater inlet for introducing seawater into a cooling chamber, and the seawater is configured to remove at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber.

[0087] In a 23rd embodiment according to any of the aforementioned embodiments, the gas conditioning system further comprises a water treatment system which is fluidly connected to a direct contact cooler and receives seawater from the direct contact cooler, the water treatment system comprising a membrane and an input system configured to adjust the pH of the seawater to greater than 6.5.

[0088] In a 24th embodiment according to any of the preceding embodiments, the gas conditioning system further comprises a rotary packed bed assembly fluidly connected to a direct contact cooler to receive flue gas from the direct contact cooler, the rotary packed bed assembly comprising a first rotary packed bed containing an absorbent configured to absorb at least a portion of carbon dioxide from the flue gas, and a second rotary packed bed configured to receive the absorbent from the first rotary packed bed and desorb the carbon dioxide absorbed from the absorbent.

[0089] In the 25th aspect according to the 24th aspect, the absorbent includes a liquid solvent.

[0090] In the 26th aspect according to the 25th aspect, the liquid solvent includes an amine solvent.

[0091] In a 27th embodiment, which is one of the 24th to 26th embodiments, the rotary bed assembly further comprises a water washing station fluidly connected to a first rotary bed, the water washing station being configured to wash flue gas from the first rotary bed with water.

[0092] In the 28th aspect according to the 27th aspect, the water washing station comprises a filling cylinder or a rotating filling bed.

[0093] In a 29th embodiment, which is any one of the 24th to 28th embodiments, the gas conditioning system further comprises a storage system fluidly connected to a second rotating packed bed, the storage system comprising a compressor and a storage tank, wherein the storage system is configured to receive desorbed carbon dioxide, compress the desorbed carbon dioxide with the compressor, and store the carbon dioxide in the storage tank.

[0094] In the 30th embodiment, a method for preparing flue gas from a ship includes the steps of: receiving exhaust flue gas from a marine engine at a temperature of 150°C to 550°C in a chamber of an oxidizer unit; converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C using reactants in the chamber of the oxidizer unit; receiving the flue gas from the oxidizer unit in a direct contact cooler; and cooling the flue gas to a temperature of 60°C or lower by bringing the flue gas into direct contact with seawater in the direct contact cooler.

[0095] In the 31st aspect according to the 30th aspect, exhaust flue gas is received from the marine engine at a temperature of 150°C to 350°C, and some of the nitrogen oxides are converted at a temperature of 150°C to 350°C.

[0096] In the 32nd aspect according to the 30th or 31st aspect, exhaust flue gas is received from the marine engine at a temperature of 150°C to 310°C, and some of the nitrogen oxides are converted at a temperature of 150°C to 310°C.

[0097] In the 33rd embodiment, which is one of the 30th to 32nd embodiments, the cooling step includes a step of cooling the flue gas to a temperature of 50°C or less.

[0098] In a 34th embodiment, which is one of the 30th to 33rd embodiments, the steps of using reactants in the chamber of an oxidizer unit to convert some of the sulfur oxides in the flue gas to sulfur dioxide and cooling the flue gas with seawater further include the step of removing at least some of the sulfur dioxide and nitrogen dioxide from the flue gas with seawater in response to direct contact between the flue gas and seawater.

[0099] In a 35th embodiment, which is one of the 30th to 34th embodiments, the oxidizer unit includes a selective catalytic reduction unit, and the conversion step includes converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C.

[0100] In a 36th aspect according to the 35th aspect, the reactant comprises a catalyst, and the step of converting a portion of nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide includes the steps of bringing the flue gas into contact with a mist of a compound solution in a chamber, and further directing the flue gas and the mist of the compound solution toward the catalyst in the chamber.

[0101] In the 37th aspect according to the 36th aspect, the compound solution includes a urea solution or an ammonia solution.

[0102] In a 38th aspect, which is one of the 35th to 37th aspects, the method further includes the steps of: receiving a cooled flue gas from a direct contact cooler in an adsorption unit; and removing at least a portion of the remaining nitrogen oxides from the cooled flue gas in an adsorption unit.

[0103] In the 39th aspect according to the 38th aspect, the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes the step of guiding the cooled flue gas through at least one adsorption bed of an adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm.

[0104] In a forty-thorough embodiment according to the thirtieth embodiment, the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through at least one adsorption bed of an adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 10 ppm.

[0105] In a 41st aspect, which is one of the 30th to 40th aspects, the method further includes the steps of increasing the pressure of flue gas using a blower unit positioned between a marine engine and an oxidizer unit, and using the blower unit to guide the flue gas to the oxidizer unit.

[0106] In a 42nd aspect, which is one of the 30th to 41st aspects, the method further includes the steps of generating a partial vacuum in the flow path of flue gas through the oxidizer unit and the direct contact cooler using a blower unit located downstream of the direct contact cooler, and using the blower unit to guide the flue gas to flow through the oxidizer unit and the blower unit toward the blower unit.

[0107] In a 43rd embodiment, which is one of any of the 30th to 42nd embodiments, the method further includes the step of filtering and removing particulate matter and volatile hydrocarbons from the flue gas using a filter located upstream of the oxidizer unit.

[0108] In a 44th embodiment, which is one of the 30th to 43rd embodiments, the direct contact cooler comprises a rotating packed bed, and the step of cooling the flue gas includes the step of directing the flue gas in the rotating packed bed into a countercurrent flow relative to the seawater in the rotating packed bed.

[0109] In the 45th aspect according to the 44th aspect, the step of directing the flue gas in the rotating packed bed into a countercurrent flow relative to the seawater in the rotating packed bed includes the step of moving at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas into the seawater.

[0110] In a 46th aspect, which is one of the 30th to 45th aspects, the method further includes the steps of introducing flue gas from a direct contact cooler to a first rotating packed bed containing an absorbent, and absorbing at least a portion of carbon dioxide from the flue gas using the absorbent in the first rotating packed bed.

[0111] In the 47th aspect according to the 46th aspect, the method further includes the steps of introducing an absorbent having absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed.

[0112] In a forty-eighth aspect according to the forty-seventh aspect, the method further includes the steps of introducing desorbed carbon dioxide into a storage system, compressing the carbon dioxide using a compressor in the storage system, and storing the compressed carbon dioxide using a storage tank in the storage system.

[0113] In a 49th aspect, which is one of the 46th to 48th aspects, the method further includes the steps of: directing flue gas from a first rotating packed bed to a water washing station having a housing surrounding a washing chamber; and washing the flue gas with water in the washing chamber of the water washing station.

[0114] In a 50th embodiment, which is one of the 30th to 49th embodiments, the step of receiving exhaust flue gas from a marine engine includes the step of receiving the exhaust flue gas at a temperature of 250°C or less, and the step of converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide includes the step of performing the conversion at a flue gas temperature of 250°C or less.

[0115] In the 51st embodiment, a gas conditioning system for removing pollutants including nitrogen oxides and sulfur oxides from a ship's flue gas includes an oxidizer unit including a first fluid inlet and a first fluid outlet, configured to receive exhaust flue gas through the first fluid inlet and to convert at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide; and a direct contact cooler having a rotating packed bed for bringing the flue gas into contact with seawater and cooling the flue gas to a temperature of 60°C or less, wherein the seawater is converted from the flue gas to... A direct contact cooler configured to remove nitrogen oxides and sulfur dioxide is provided, and a rotating packed bed comprises a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing, a first fluid outlet of the oxidizer unit, and a second fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet.

[0116] In the 52nd aspect according to the 51st aspect, the flue gas is arranged in a countercurrent flow relative to the seawater in the rotor drum when the rotating packed bed is in use.

[0117] In the 53rd aspect according to the 51st or 52nd aspect, the seawater inlet is configured such that the seawater inlet leads seawater into the rotor drum and the seawater removes at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber.

[0118] In the 54th embodiment, which is one of the 51st to 53rd embodiments, the oxidizer unit comprises a selective catalytic reduction unit, the selective catalytic reduction unit receives exhaust flue gas at a temperature of 150°C to 350°C, and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C.

[0119] In the 55th aspect according to the 54th aspect, the selective catalytic reduction unit comprises a second housing defining a second chamber and a compound inlet configured to introduce a mist of compound solution into the second chamber, wherein a first fluid inlet is configured to guide a flue gas into contact with the mist of compound solution in the second chamber.

[0120] In the 56th aspect according to the 55th aspect, the compound solution contains urea or ammonia.

[0121] In the 57th embodiment according to the 55th or 56th embodiment, the selective catalytic reduction unit comprises a catalyst located in a second chamber, wherein the catalyst is configured to come into contact with flue gas and a mist of compound solution in the second chamber.

[0122] In a 58th aspect according to the 57th aspect, the gas conditioning system further comprises an adsorption unit including a third fluid inlet fluidly connected to a second fluid outlet of a direct contact cooler, wherein the adsorption unit is configured to receive flue gas from the direct contact cooler and remove at least a portion of the remaining nitrogen oxides from the flue gas from the direct contact cooler.

[0123] In the 59th aspect according to the 58th aspect, the adsorption unit comprises at least one adsorption bed, and the gas conditioning system is configured to guide flue gas from a third fluid inlet through at least one adsorption bed, wherein the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

[0124] In the 60th aspect according to the 59th aspect, the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

[0125] In the 61st aspect according to the 59th or 60th aspect, the adsorption unit comprises two adsorption beds.

[0126] In the 62nd embodiment, which is one of the 51st to 61st embodiments, the gas conditioning system further comprises a filter located upstream of the first fluid inlet, the filter configured to remove particulate matter and volatile hydrocarbons from the flue gas.

[0127] In the 63rd aspect according to the 62nd aspect, the filter is directly coupled to the oxidizer unit at the first fluid inlet of the oxidizer unit.

[0128] In the 64th embodiment, which is one of the 51st to 63rd embodiments, the gas conditioning system further comprises a blower unit located upstream of a first fluid inlet of an oxidizer unit, the blower unit being configured to guide flue gas into the oxidizer unit and increase the pressure of the flue gas.

[0129] In a 65th embodiment, which is one of the 51st to 64th embodiments, the gas conditioning system further comprises a blower unit located downstream of a direct contact cooler, the blower unit being configured to generate a partial vacuum in the flow path of flue gas through the oxidizer unit and the direct contact cooler, thereby facilitating the flow of flue gas through the oxidizer and the direct contact cooler toward the blower unit.

[0130] In a 66th embodiment, which is any one of the 51st to 65th embodiments, the gas conditioning system further comprises a rotary packed bed assembly fluidly connected to a direct contact cooler to receive flue gas from the direct contact cooler, the rotary packed bed assembly comprising a first rotary packed bed containing an absorbent configured to absorb at least a portion of carbon dioxide from the flue gas, and a second rotary packed bed configured to receive the absorbent from the first rotary packed bed and desorb the carbon dioxide absorbed from the absorbent.

[0131] In the 67th aspect according to the 66th aspect, the rotary bed assembly further comprises a water washing station fluidly connected to a first rotary bed, the water washing station being configured to wash flue gas from the first rotary bed with water.

[0132] In the 68th aspect according to the 67th aspect, the water washing station comprises a filling cylinder or a rotating filling bed.

[0133] In the 69th embodiment, which is one of the 66th to 68th embodiments, the gas conditioning system further comprises a storage system fluidly connected to a second rotating packed bed, the storage system comprising a compressor and a storage tank, wherein the storage system is configured to receive desorbed carbon dioxide, compress the desorbed carbon dioxide with the compressor, and store the carbon dioxide in the storage tank.

[0134] In the 70th embodiment, which is one of the 51st to 69th embodiments, the rotating packed bed of the direct contact cooler brings the flue gas into contact with seawater and cools the flue gas to a temperature of 50°C or less.

[0135] In the 71st embodiment, a method for preparing flue gas includes the steps of: receiving exhaust flue gas in a chamber of an oxidizer unit; converting a portion of nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide using reactants in the chamber of the oxidizer unit; receiving flue gas from the oxidizer unit in a direct contact cooler, wherein the direct contact cooler includes a rotating packed bed; and cooling the flue gas in the rotating packed bed to a temperature of 60°C or less by bringing it into contact with seawater in the rotating packed bed.

[0136] In the 72nd aspect according to the 71st aspect, the step of converting using reactants in the chamber of an oxidizer unit further includes the step of converting a portion of the sulfur oxides in the flue gas into sulfur dioxide, and the step of bringing the flue gas in the rotating packed bed into contact with seawater in the rotating packed bed includes the step of transferring at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas into the seawater.

[0137] In the 73rd aspect according to the 71st or 72nd aspect, the oxidizer unit includes a selective catalytic reduction unit, the step of receiving exhaust flue gas includes receiving exhaust flue gas in the chamber of the selective catalytic reduction unit at a temperature of 150°C to 550°C, and the step of converting a portion of nitrogen oxides includes converting a portion of nitrogen oxides into nitrogen gas at a temperature of 150°C to 550°C.

[0138] In the 74th aspect according to the 73rd aspect, the step of receiving exhaust flue gas includes receiving exhaust flue gas in a chamber of a selective catalytic reduction unit at a temperature of 150°C to 350°C, and the step of converting a portion of nitrogen oxides includes converting a portion of nitrogen oxides into nitrogen gas at a temperature of 150°C to 350°C.

[0139] In the 75th aspect according to the 74th aspect, the step of receiving exhaust flue gas includes receiving exhaust flue gas in a chamber of a selective catalytic reduction unit at a temperature of 150°C to 310°C, and the step of converting a portion of nitrogen oxides includes converting a portion of nitrogen oxides into nitrogen gas at a temperature of 150°C to 310°C.

[0140] In a 76th aspect, which is any one of the 71st to 75th aspects, the reactant includes a catalyst, and the step of converting a portion of the nitrogen oxides into nitrogen gas includes the step of bringing a flue gas into contact with a mist of the compound solution in the chamber, and the step of further directing the flue gas and the mist of the compound solution toward the catalyst in the chamber.

[0141] In the 77th aspect according to the 76th, the compound solution includes a urea solution or an ammonia solution.

[0142] In the 78th aspect, which is one of the 71st to 77th aspects, the method further includes the steps of: receiving a cooled flue gas from a direct contact cooler in an adsorption unit; and removing at least a portion of the remaining nitrogen oxides from the cooled flue gas in an adsorption unit.

[0143] In the 79th aspect according to the 78th aspect, the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through at least one adsorption bed of an adsorption unit to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

[0144] In the 80th aspect according to the 79th aspect, the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes the step of guiding the cooled flue gas through at least one adsorption bed of an adsorption unit to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

[0145] In the 81st aspect, which is one of the 71st to 80th aspects, the method further includes the steps of increasing the pressure of flue gas using a blower unit located upstream of the oxidizer unit, and guiding the flue gas to the oxidizer unit using the blower unit.

[0146] In an 82nd aspect, which is one of any of the 71st to 81st aspects, the method further includes the steps of generating a partial vacuum in the flow path of flue gas through the oxidizer unit and the direct contact cooler using a blower unit located downstream of the direct contact cooler, and using a blower unit to guide the flue gas to flow through the oxidizer unit and the blower unit toward the blower unit.

[0147] In an 83rd aspect, which is one of any of the 71st to 82nd aspects, the method further includes the step of filtering and removing particulate matter and volatile hydrocarbons from the flue gas using a filter located upstream of the oxidizer unit.

[0148] In an 84th aspect, which is one of any of the 71st to 83rd aspects, the method further includes the steps of: introducing flue gas from a direct contact cooler to a first rotating packed bed containing an absorbent; and absorbing at least a portion of carbon dioxide from the flue gas using the absorbent in the first rotating packed bed.

[0149] In the 85th aspect according to the 84th aspect, the method further includes the steps of introducing an absorbent having absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed.

[0150] In the 86th aspect according to the 85th aspect, the method further includes the steps of introducing desorbed carbon dioxide into a storage system, compressing the carbon dioxide using a compressor in the storage system, and storing the compressed carbon dioxide using a storage tank in the storage system.

[0151] In an 87th aspect, which is one of any of the 84th to 86th aspects, the method further includes the steps of: directing flue gas from a first rotating packed bed to a water washing station having a housing surrounding a washing chamber; and washing the flue gas with water in the washing chamber of the water washing station.

[0152] In an 88th embodiment, which is one of any of the 71st to 87th embodiments, the step of guiding the flue gas in the rotating packed bed to come into contact with the seawater in the rotating packed bed includes the step of guiding the flue gas into a countercurrent flow relative to the seawater in the rotating packed bed.

[0153] In the 89th embodiment, which is one of any of the 71st to 88th embodiments, the step of guiding the flue gas in the rotating packed bed into contact with the seawater in the rotating packed bed cools the flue gas to a temperature of 50°C or less.

[0154] In the 90th aspect, the vessel is equipped with a gas adjustment system of any of the aforementioned aspects.

[0155] Therefore, this specification and the drawings should be considered illustrative rather than restrictive. Furthermore, the foregoing use of embodiments and other exemplary language does not necessarily refer to the same embodiment or example, but may refer to different distinct embodiments, as well as potentially the same embodiment. The above specification has described in detail with reference to specific exemplary embodiments. However, it will be apparent that various modifications and changes can be made without departing from the broader spirit and scope of this disclosure as set forth in the claims.

Claims

1. A gas conditioning system for removing pollutants, including nitrogen oxides and sulfur oxides, from the flue gas of a ship, An oxidizer unit including a first fluid inlet and a first fluid outlet, configured to receive exhaust flue gas from a marine engine through the first fluid inlet at a temperature of 150°C to 550°C, and configured to convert at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C, A gas conditioning system comprising: a direct contact cooler including a second fluid inlet fluidly connected to the first fluid outlet of the oxidizer unit, a housing defining a cooling chamber, and a second fluid outlet, the direct contact cooler configured to cool the flue gas to a temperature of 60°C or less by bringing the flue gas into contact with seawater present in the cooling chamber, and the seawater configured to remove nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber.

2. The gas conditioning system according to claim 1, wherein the oxidizer unit is configured to receive the exhaust flue gas from the marine engine through the first fluid inlet at a temperature of 150°C to 350°C, and the oxidizer unit is configured to convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C.

3. The gas adjustment system according to claim 1 or 2, wherein the direct contact cooler is configured to cool the flue gas to a temperature of 50°C or less.

4. The gas conditioning system according to any one of claims 1 to 3, wherein the oxidizer unit is configured to receive the exhaust flue gas from the marine engine through the first fluid inlet at a temperature of 150°C to 310°C, and the oxidizer unit is configured to convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 310°C.

5. The gas conditioning system according to any one of claims 1 to 4, wherein the oxidizer unit is further configured to convert at least a portion of the sulfur oxides in the flue gas to sulfur dioxide at a temperature of 150°C to 550°C, and the direct contact cooler is configured to separate the nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber.

6. The gas conditioning system according to any one of claims 1 to 5, wherein the oxidizer unit comprises a housing defining an oxidation chamber and an oxidizing agent present in the oxidation chamber, and the oxidizing agent is configured to be in direct contact with the exhaust flue gas.

7. The gas conditioning system according to claim 6, wherein the oxidizing agent comprises a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite, and the solution is configured to come into contact with the flue gas and convert at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide.

8. The gas adjustment system according to any one of claims 1 to 7, wherein the oxidizer unit comprises a selective catalytic reduction unit configured to convert a portion of the nitrogen oxides into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C.

9. The gas conditioning system according to claim 8, further comprising an adsorption unit including a third fluid inlet fluidly connected to the second fluid outlet of the direct contact cooler, wherein the adsorption unit is configured to receive the flue gas from the direct contact cooler and remove at least a portion of the remaining nitrogen oxides from the flue gas from the direct contact cooler.

10. The gas conditioning system according to claim 9, wherein the adsorption unit comprises at least one adsorption bed, the gas conditioning system is configured to guide the flue gas from the third fluid inlet through the at least one adsorption bed, and the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

11. The gas adjustment system according to claim 10, wherein the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

12. The gas adjustment system according to claim 10 or claim 11, wherein the adsorption unit comprises two adsorption beds.

13. The gas conditioning system according to any one of claims 8 to 12, wherein the selective catalytic reduction unit comprises a second housing defining a second chamber and a compound inlet configured to introduce a mist of a compound solution into the second chamber, and the first fluid inlet is configured to guide the flue gas into contact with the compound solution in the second chamber.

14. The gas adjustment system according to claim 13, wherein the compound solution contains urea or ammonia.

15. The gas adjustment system according to claim 13 or 14, wherein the selective catalytic reduction unit comprises a catalyst disposed in the second chamber, and the catalyst is configured to come into contact with the flue gas and the mist of the compound solution.

16. The gas conditioning system according to any one of claims 1 to 15, further comprising a filter located upstream of the first fluid inlet, wherein the filter is configured to remove particulate matter and volatile hydrocarbons from the flue gas.

17. The gas conditioning system according to claim 16, wherein the filter is directly coupled to the oxidizer unit at the first fluid inlet of the oxidizer unit.

18. The gas regulating system according to any one of claims 1 to 17, further comprising a blower unit positioned between a marine engine and the first fluid inlet of the oxidizer unit, wherein the blower unit is configured to guide the flue gas to the oxidizer unit and increase the pressure of the flue gas.

19. The gas conditioning system according to any one of claims 1 to 18, further comprising a blower unit disposed downstream of the direct contact cooler, wherein the blower unit is configured to generate a partial vacuum in the flow path of the flue gas through the oxidizer and the direct contact cooler, thereby facilitating the flow of the flue gas through the oxidizer and the direct contact cooler toward the blower unit.

20. The direct contact cooler is equipped with a rotating filling bed, and the rotating filling bed is The housing surrounding the cooling chamber, A rotor drum disposed within the housing and rotatable around a rotation axis, and a seawater inlet fluid connected to the rotor drum, A seawater outlet is fluid-connected to the housing, The housing comprises a second fluid inlet fluid-connected to the housing and a second fluid outlet fluid-connected to the rotor drum, The gas adjustment system according to any one of claims 1 to 19, wherein the flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet.

21. The gas adjustment system according to claim 20, wherein the flue gas is arranged in a countercurrent flow relative to the seawater in the rotor drum when the rotating packed bed is in use.

22. The gas conditioning system according to any one of claims 1 to 21, wherein the direct contact cooler includes a seawater inlet for introducing the seawater into the cooling chamber, and the seawater is configured to remove at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber.

23. The gas adjustment system according to any one of claims 1 to 22, further comprising a water treatment system which is fluidly connected to the direct contact cooler and receives the seawater from the direct contact cooler, wherein the water treatment system comprises a membrane and an input system configured to adjust the pH of the seawater to be greater than 6.

5.

24. The rotary filling bed assembly is further fluidly connected to the direct contact cooler to receive the flue gas from the direct contact cooler, and the rotary filling bed assembly is A first rotating packed bed comprising an absorbent configured to absorb at least a portion of carbon dioxide from the flue gas, A gas adjustment system according to any one of claims 1 to 23, comprising: a second rotating packed bed configured to receive the absorbent from the first rotating packed bed and to desorb the absorbed carbon dioxide from the absorbent.

25. The gas adjustment system according to claim 24, wherein the absorbent comprises a liquid solvent.

26. The gas adjustment system according to claim 25, wherein the liquid solvent comprises an amine solvent.

27. The gas conditioning system according to any one of claims 24 to 26, wherein the rotating bed assembly further comprises a water washing station fluidly connected to the first rotating bed, the water washing station being configured to wash the flue gas from the first rotating bed with water.

28. The gas adjustment system according to claim 27, wherein the water washing station comprises a filling cylinder or a rotating filling bed.

29. The gas adjustment system according to any one of claims 24 to 28, further comprising a storage system fluidly connected to the second rotating packed bed, the storage system being configured to receive desorbed carbon dioxide, compress the desorbed carbon dioxide with the compressor, and store the carbon dioxide in the storage tank.

30. A method for adjusting flue gas from a ship, comprising the steps of receiving exhaust flue gas from a marine engine at a temperature of 150°C to 550°C in the chamber of an oxidizer unit, A step of using the reactant in the chamber of the oxidizer unit to convert a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C, In a direct contact cooler, the steps include receiving the flue gas from the oxidizer unit, A method comprising the step of bringing the flue gas into direct contact with seawater in the direct contact cooler to cool the flue gas to a temperature of 60°C or lower.

31. The exhaust flue gas is received from the marine engine at a temperature of 150°C to 350°C. The method according to claim 30, wherein a portion of the nitrogen oxide is converted at a temperature of 150°C to 350°C.

32. The exhaust flue gas is received from the marine engine at a temperature of 150°C to 310°C. The method according to claim 30 or claim 31, wherein the portion of the nitrogen oxide is converted at a temperature of 150°C to 310°C.

33. The method according to any one of claims 30 to 32, wherein the cooling step includes a step of cooling the flue gas to a temperature of 50°C or less.

34. The steps include: using the reaction material in the chamber of the oxidizer unit to convert a portion of the sulfur oxides in the flue gas into sulfur dioxide, The step of cooling the flue gas with seawater further includes the step of removing at least a portion of the sulfur dioxide and nitrogen dioxide from the flue gas with the seawater in response to the direct contact between the flue gas and the seawater. The method according to any one of claims 30 to 33.

35. The method according to any one of claims 30 to 34, wherein the oxidizer unit includes a selective catalytic reduction unit, and the conversion step includes converting the portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C.

36. The method according to claim 35, wherein the reactant comprises a catalyst, and the step of converting the portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide includes the steps of bringing the flue gas into contact with a mist of the compound solution in the chamber, and further directing the flue gas and the mist of the compound solution toward the catalyst in the chamber.

37. The method according to claim 36, wherein the compound solution comprises a urea solution or an ammonia solution.

38. The adsorption unit includes the steps of receiving the cooled flue gas from the direct contact cooler, and removing at least a portion of the remaining nitrogen oxides from the cooled flue gas. The method according to any one of claims 35 to 37, further comprising:

39. The method according to claim 38, wherein the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm.

40. The method according to claim 39, wherein the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes the step of guiding the cooled flue gas through the at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 10 ppm.

41. The steps include increasing the pressure of the flue gas using a blower unit positioned between the marine engine and the oxidizer unit, The steps include using the blower unit to guide the flue gas to the oxidizer unit, The method according to any one of claims 30 to 40, further comprising:

42. A step of generating a partial vacuum in the flow path of the flue gas passing through the oxidizer unit and the direct contact cooler using a blower unit positioned downstream of the direct contact cooler, The steps include using the blower unit to guide the flue gas through the oxidizer unit and the blower unit so that it flows toward the blower unit, The method according to any one of claims 30 to 41, further comprising:

43. The method according to any one of claims 30 to 42, further comprising the step of filtering and removing particulate matter and volatile hydrocarbons from the flue gas using a filter located upstream of the oxidizer unit.

44. The method according to any one of claims 30 to 43, wherein the direct contact cooler comprises a rotating packed bed, and the step of cooling the flue gas includes the step of directing the flue gas in the rotating packed bed into a countercurrent flow relative to the seawater in the rotating packed bed.

45. The method according to claim 44, wherein the step of directing the flue gas in the rotating packed bed into a countercurrent flow relative to the seawater in the rotating packed bed includes the step of moving at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas to the seawater.

46. The steps include: guiding the flue gas from the direct contact cooler to a first rotating packed bed containing an absorbent; The steps include using the absorbent in the first rotating bed to absorb at least a portion of the carbon dioxide from the flue gas, The method according to any one of claims 30 to 45, further comprising:

47. The steps include: guiding the absorbent having absorbed carbon dioxide to a second rotating packed bed; In the second rotating packed bed, the steps include desorbing the absorbed carbon dioxide from the absorbent, The method according to claim 46, further comprising:

48. The steps include: guiding the desorbed carbon dioxide into a storage system; The steps include: compressing the carbon dioxide using the compressor of the storage system, and storing the compressed carbon dioxide using the storage tank of the storage system. The method according to claim 47, further comprising:

49. The steps include: guiding the flue gas from the first rotating filling bed to a water washing station equipped with a housing surrounding the washing chamber; The steps include: washing the flue gas with water in the washing chamber of the water washing station, The method according to any one of claims 46 to 48, further comprising:

50. The step of receiving the exhaust flue gas from the marine engine includes the step of receiving the exhaust flue gas at a temperature of 250°C or less. The method according to any one of claims 30 to 49, wherein the step of converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide includes the step of performing the conversion at a temperature of the flue gas of 250°C or less.

51. A gas conditioning system for removing pollutants, including nitrogen oxides and sulfur oxides, from the flue gas of a ship, An oxidizer unit including a first fluid inlet and a first fluid outlet, configured to receive exhaust flue gas through the first fluid inlet, and configured to convert at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide, A direct contact cooler comprising a rotating packed bed for bringing the flue gas into contact with seawater and cooling the flue gas to a temperature of 60°C or less, wherein the seawater is configured to remove nitrogen dioxide and sulfur dioxide from the flue gas, and the rotating packed bed is The housing surrounding the cooling chamber, A rotor drum disposed within the housing and rotatable around a rotation axis, and a seawater inlet fluid connected to the rotor drum, A seawater outlet is fluid-connected to the housing, The housing and the first fluid outlet of the oxidizer unit are fluid-connected to a second fluid inlet, The rotor drum is equipped with a second fluid outlet that is fluidly connected to the rotor drum, A gas adjustment system in which the flue gas is guided from the second fluid inlet to the second fluid outlet, and the seawater is guided from the seawater inlet to the seawater outlet.

52. The gas adjustment system according to claim 51, wherein the flue gas is arranged in a countercurrent flow relative to the seawater in the rotor drum when the rotating filled bed is in use.

53. The gas conditioning system according to claim 51 or 52, wherein the seawater inlet is configured to guide the seawater into the rotor drum, and the seawater removes at least a portion of the sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber.

54. The gas adjustment system according to any one of claims 51 to 53, wherein the oxidizer unit comprises a selective catalytic reduction unit, the selective catalytic reduction unit receives the exhaust flue gas at a temperature of 150°C to 350°C, and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C.

55. The gas conditioning system according to claim 54, wherein the selective catalytic reduction unit comprises a second housing defining a second chamber and a compound inlet configured to introduce a mist of a compound solution into the second chamber, and the first fluid inlet is configured to guide the flue gas into contact with the mist of the compound solution in the second chamber.

56. The gas adjustment system according to claim 55, wherein the compound solution contains urea or ammonia.

57. The gas adjustment system according to claim 55 or claim 56, wherein the selective catalytic reduction unit comprises a catalyst disposed in the second chamber, and the catalyst is configured to come into contact with the flue gas and the mist of the compound solution in the second chamber.

58. The adsorption unit further includes a third fluid inlet fluid-connected to the second fluid outlet of the direct contact cooler, wherein the adsorption unit is configured to receive the flue gas from the direct contact cooler and remove at least a portion of the remaining nitrogen oxides from the flue gas from the direct contact cooler. The gas adjustment system according to claim 57.

59. The gas conditioning system according to claim 58, wherein the adsorption unit comprises at least one adsorption bed, the gas conditioning system is configured to guide the flue gas from the third fluid inlet through the at least one adsorption bed, and the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

60. The gas adjustment system according to claim 59, wherein the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

61. The gas adjustment system according to claim 59 or 60, wherein the adsorption unit comprises two adsorption beds.

62. The gas conditioning system according to any one of claims 51 to 61, further comprising a filter located upstream of the first fluid inlet, wherein the filter is configured to remove particulate matter and volatile hydrocarbons from the flue gas.

63. The gas conditioning system according to claim 62, wherein the filter is directly coupled to the oxidizer unit at the first fluid inlet of the oxidizer unit.

64. The gas regulating system according to any one of claims 51 to 63, further comprising a blower unit located upstream of the first fluid inlet of the oxidizer unit, wherein the blower unit is configured to guide the flue gas to the oxidizer unit and increase the pressure of the flue gas.

65. The gas conditioning system according to any one of claims 51 to 64, further comprising a blower unit located downstream of the direct contact cooler, wherein the blower unit is configured to generate a partial vacuum in the flow path of the flue gas through the oxidizer unit and the direct contact cooler, thereby facilitating the flow of the flue gas through the oxidizer and the direct contact cooler toward the blower unit.

66. The rotary filling bed assembly is further fluidly connected to the direct contact cooler to receive the flue gas from the direct contact cooler, and the rotary filling bed assembly is A first rotating packed bed comprising an absorbent configured to absorb at least a portion of the carbon dioxide from the flue gas, A gas adjustment system according to any one of claims 51 to 65, comprising: a second rotating packed bed configured to receive the absorbent from the first rotating packed bed and to desorb the absorbed carbon dioxide from the absorbent.

67. The gas conditioning system according to claim 66, wherein the rotary bed assembly further comprises a water washing station fluidly connected to the first rotary bed, the water washing station being configured to wash the flue gas from the first rotary bed with water.

68. The gas adjustment system according to claim 67, wherein the water washing station comprises a filling cylinder or a rotating filling bed.

69. The gas adjustment system according to any one of claims 66 to 68, further comprising a storage system fluidly connected to the second rotating packed bed, the storage system being configured to receive desorbed carbon dioxide, compress the desorbed carbon dioxide with the compressor, and store the carbon dioxide in the storage tank.

70. The gas adjustment system according to any one of claims 51 to 69, wherein the rotating packed bed of the direct contact cooler brings the flue gas into contact with seawater and cools the flue gas to a temperature of 50°C or less.

71. A method for adjusting flue gas, comprising the steps of receiving exhaust flue gas in the chamber of an oxidizer unit, A step of using the reactant in the chamber of the oxidizer unit to convert a portion of the nitrogen oxides in the flue gas into nitrogen gas or at least one of nitrogen dioxide, A step in a direct contact cooler, comprising receiving the flue gas from the oxidizer unit, wherein the direct contact cooler includes a rotating packed bed, A method comprising the step of bringing the flue gas in the rotating packed bed into contact with seawater in the rotating packed bed to cool the flue gas to a temperature of 60°C or lower.

72. The step of using the reactant in the chamber of the oxidizer unit to perform the conversion further includes the step of converting a portion of the sulfur oxides in the flue gas into sulfur dioxide, The step of bringing the flue gas in the rotating packed bed into contact with the seawater in the rotating packed bed includes the step of transferring at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas to the seawater. The method according to claim 71.

73. The oxidizer unit includes a selective catalytic reduction unit, The step of receiving the exhaust flue gas includes receiving the exhaust flue gas in the chamber of the selective catalytic reduction unit at a temperature of 150°C to 550°C. The step of converting the portion of the nitrogen oxide includes the step of converting the portion of the nitrogen oxide into nitrogen gas at a temperature of 150°C to 550°C. The method according to claim 71 or claim 72.

74. The step of receiving the exhaust flue gas includes receiving the exhaust flue gas in the chamber of the selective catalytic reduction unit at a temperature of 150°C to 350°C. The step of converting the portion of the nitrogen oxide includes the step of converting the portion of the nitrogen oxide into nitrogen gas at a temperature of 150°C to 350°C. The method according to claim 73.

75. The step of receiving the exhaust flue gas includes receiving the exhaust flue gas in the chamber of the selective catalytic reduction unit at a temperature of 150°C to 310°C. The step of converting the portion of the nitrogen oxide includes the step of converting the portion of the nitrogen oxide into nitrogen gas at a temperature of 150°C to 310°C. The method according to claim 74.

76. The method according to any one of claims 71 to 75, wherein the reactant comprises a catalyst, and the step of converting the portion of the nitrogen oxide into nitrogen gas comprises the step of directing the flue gas to contact a mist of the compound solution in the chamber, and the step of further directing the flue gas and the mist of the compound solution toward the catalyst in the chamber.

77. The method according to claim 76, wherein the compound solution comprises a urea solution or an ammonia solution.

78. In the adsorption unit, the steps include receiving the cooled flue gas from the direct contact cooler, The adsorption unit includes the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas, The method according to any one of claims 71 to 77, further comprising:

79. The method according to claim 78, wherein the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

80. The method according to claim 79, wherein the step of removing at least a portion of the remaining nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through the at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

81. The steps include increasing the pressure of the flue gas using a blower unit located upstream of the oxidizer unit, The steps include using the blower unit to guide the flue gas to the oxidizer unit, The method according to any one of claims 71 to 80, further comprising:

82. A step of generating a partial vacuum in the flow path of the flue gas passing through the oxidizer unit and the direct contact cooler using a blower unit positioned downstream of the direct contact cooler, The steps include using the blower unit to guide the flue gas through the oxidizer unit and the blower unit so that it flows toward the blower unit, The method according to any one of claims 71 to 81, further comprising:

83. The method according to any one of claims 71 to 82, further comprising the step of filtering and removing particulate matter and volatile hydrocarbons from the flue gas using a filter located upstream of the oxidizer unit.

84. The steps include: guiding the flue gas from the direct contact cooler to a first rotating packed bed containing an absorbent; The steps include using the absorbent in the first rotating bed to absorb at least a portion of the carbon dioxide from the flue gas, The method according to any one of claims 71 to 83, further comprising:

85. The steps include: guiding the absorbent having absorbed carbon dioxide to a second rotating packed bed; In the second rotating packed bed, the steps include desorbing the absorbed carbon dioxide from the absorbent, The method according to claim 84, further comprising:

86. The steps include: guiding the desorbed carbon dioxide into a storage system; The steps include: compressing the carbon dioxide using the compressor of the storage system, and storing the compressed carbon dioxide using the storage tank of the storage system. The method according to claim 85, further comprising:

87. The steps include: guiding the flue gas from the first rotating filling bed to a water washing station equipped with a housing surrounding the washing chamber; The steps include: washing the flue gas with water in the washing chamber of the water washing station, The method according to any one of claims 84 to 86, further comprising:

88. The method according to any one of claims 71 to 87, wherein the step of guiding the flue gas in the rotating packed bed to come into contact with the seawater in the rotating packed bed includes the step of guiding the flue gas into a countercurrent flow relative to the seawater in the rotating packed bed.

89. The method according to any one of claims 71 to 88, wherein the step of guiding the flue gas in the rotating packed bed into contact with seawater in the rotating packed bed is to cool the flue gas to a temperature of 50°C or less.

90. A vessel comprising a gas adjustment system according to any one of claims 1 to 29, or any one of claims 51 to 70.

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