Gas liquid contactor and effluent cleaning system and method

The present invention is under the name "Two Phase Reactor", which is a continuation of US Patent Application No. 11 / 057,539 (currently Patent No. 7,379,487) filed on February 14, 2005 under the name "Two Phase Reactor". A partial continuation of US Patent Application No. 12 / 012,568 filed on February 4, 2008, and a US provisional application filed on September 26, 2008 under the name "System for Gaseous Pollutant Removal". 61 / 100,564, US Provisional Application No. 61 / 100,606 filed on September 26, 2008 under the name "Liquid Gas Contactor System and Method", 2008 under the name "Liquid Gas Contactor and Effluent Cleaning System and Method" Claiming the benefits of US Provisional Application No. 61 / 100,591 filed on September 26, 2014, all of these disclosures are incorporated herein by reference.

The present invention relates to a gas-liquid contactor and an exhaust cleaning system and method, and more particularly, to maximize the interaction between airflow and liquid flow while minimizing disturbance from gas-liquid during high-speed replenishment of liquid. The present invention relates to a nozzle array that produces a plurality of uniformly spaced flat liquid jets having a shape capable of being formed.

Absorption of gas into a liquid is an important processing step in various gas-liquid contact systems. Airflow contactors, also known as gas-liquid reactors, are classified into surface reactors and volumetric reactors, each of which forms an interfacial surface area between two phases on the surface of the liquid and in the bulk liquid. There are numerous examples of surface gas-liquid reactors such as rotating discs and liquid jet contactors. A rotating disc generator is a disc (rotor) that is partially immersed in a liquid and exposed to airflow. A thin film of solution is formed on the surface of the rotor and comes into contact with the parallel reagent stream. Rotate the disc to renew the contact of the liquid reagent with the gas. In the volume-type gas-liquid reactor, the gas phase is dispersed in the bulk liquid as fine bubbles. The shape of the bubbles may be spherical or irregular, and is introduced into the liquid by a gas sparger. Bubbles can be mechanically disturbed to promote mass transfer.

In many gas-liquid contact systems, the transport rate of the gas to the liquid phase is controlled by the liquid phase mass transfer rate k between the bulk fluid and the gas-liquid interface, the interface surface area A, and the concentration gradient ΔC. Therefore, the general form of the absorption rate of gas into a liquid is expressed as follows.<maths num="1"><img id="000002" he="17" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></maths> Here, the variable Φ is the gas absorption rate per unit volume of the reactor (mol / cm).³), And φ is the average absorption rate per unit boundary area (mol / cm).²), And a is the gas-liquid boundary area per unit volume (cm)²/cm³, Or cm^-1), P and pi are the partial pressures (bars) of the bulk gas and the reagent gas at the interface, C_L^*Is the concentration on the liquid side (molar / cm) that is the equilibrium point with the existing gas phase concentration pi.³) And C_L(Mole / cm³) Is the average concentration of dissolved gas in the bulk liquid, k_GAnd k_LIs the mass transfer coefficient (cm / s) on the gas side and the liquid side, respectively.

In related techniques, there are many methods for maximizing mass transfer and specific surface area in gas contactor systems. The main methods include gas spargers, wet wall jets, spraying or atomization. Which gas-liquid contactor is selected depends on the reaction conditions such as airflow / liquid flow, mass transfer, and the nature of the chemical reaction. Table 1 summarizes the various mass transfer characteristics of gas-liquid reactors in some related technologies. To optimize the gas absorption rate, the parameter k_L, A, and (C_L^*-C_L) Needs to be maximized. In many gas-liquid reaction systems, C_L^*There is a limit to the control of the concentration gradient due to the very low solubility of. Therefore, the primary parameters in the design of an efficient gas-liquid flow reactor are mass transfer and the ratio of interfacial surface area to the volume of the reactor (also known as specific surface area).<tables num="1"><img id="000003" he="78" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

Many gas-liquid contact devices have characteristics that depend on the interface contact area. For example, by using a chemical oxygen iodine laser (COIL), chlorine gas (Cl)₂) And a chemical fuel consisting of basic hydrogen peroxide (BHP) produces laser energy. This reaction produces singlet delta oxygen that powers COIL. This technology is Cl₂A circular jet of liquid BHP mixed with gas is used to generate this singlet delta oxygen. In a typical generator, the jet has a diameter on the order of 350 microns or less. The liquid BHP is pressed at high density by the pressure of a nozzle plate containing holes to generate a jet. As a result, Cl₂The interfacial surface area in contact with the gas increases. The larger the surface area, the smaller the generator and the higher the yield of excitation oxygen that can be supplied to the laser cavity. Smaller, denser-filled jets increase the specific surface area, but also increase clogging and breakage. Clogs are important because the reaction of chlorine with basic hydrogen peroxide produces the chlorine salt of the alkali metal hydroxide used to produce the basic hydrogen peroxide. It's a problem. Further clogging limits the molar concentration range of basic hydrogen peroxide, reducing the yield of singlet oxygen and laser power. The heaviest element in the COIL system is this chemical fuel. Problems inherent in fuel production increase the overall weight and efficiency of the COIL laser. Therefore, it is desired to provide a COIL laser that is more efficient and lighter than the current design.

As another example, gas-liquid contactors are also used in aerobic fermentation processes. One of the most important reagents in this aerobic fermentation is oxygen. The solubility in the aqueous solution is low, but it needs to be high to maintain the culture. In a commercially available fermenter (&gt; 10,000 L), the bubble dispersion is agitated and the volume mass transfer coefficient k_LaIs raising. Upon agitation, the dissolved oxygen travels throughout the bulk fluid, breaking the coalescence of bubbles and reducing the boundary layer surrounding the bubbles. The boundary area in these systems can be increased by increasing the number of bubbles in the reactor and reducing the diameter of the bubbles. However, microbial mass transfer is still constrained by the relatively small interfacial surface area of bubbles and the short bubble retention times. In the current sparger system (bubble dispersion), the volume mass transfer coefficient k_LaIs relatively small at about 0.2 / s, so it is desired to develop a new method that can generate the maximum interfacial surface area and overcome these restrictions on mass transfer.

Both cost and efficiency must be taken into account when designing an industrially usable system. None of the conventional methods generally satisfy both of these requirements. For example, the industrial use of conventional gas-liquid contacts requires the reaction or dissolution of gas phase chemicals with the liquid phase in chemical treatment, industrial biological applications, pollution control, or dynamic flow systems. It was decided that the process would be similar.

Taking pollution control as an example, the standard method for wet removal of a compound of interest (s) is backflow using tiny droplets of a liquid phase that falls 180 degrees opposite to the flowing gas phase. It is a system. Gravity is typically used to introduce the liquid phase into the tower or the capture sump at the base of the tower. The gas phase flows through the same tower or tower. It then captures this gas phase for further processing or release to the atmosphere.

To allow for larger scale chemical treatments, the length or diameter of the tower or tower needs to be adjusted to be linearly proportional to the size of the desired treatment. The current theoretical method is to increase the size per unit process because the cost of capital per unit process is not linearly proportional to the size.

Another drawback of standard backflow systems is that in gravity or spray / droplet gas-liquid contactors, the velocity of the airflow must be slow enough so that the effect of gravity is greater than the buoyancy of the droplet. is there. It is necessary to capture most of this water vapor prior to secondary treatment or release, regardless of the evaporation of most of the liquid reagent due to the long contact time.

Accordingly, the present invention relates to gas-liquid contactors and exhaust cleaning systems and methods that can substantially eliminate one or more problems due to the limitations and shortcomings present in the related art.

One advantage of the present invention is that it provides a large volume mass transfer coefficient, which in turn allows for a small low pressure sorbent process with minimal pumping functionality throughout the system.

Another advantage of the present invention is that it is possible to provide a gas-liquid contactor with a system footprint smaller than that of the related art.

Another advantage of the present invention is that a gas-liquid contactor can be provided in a modular design.

Another advantage of the present invention is that the performance of the gas-liquid reactor can be improved by increasing the specific surface area of the flat jet (for example, a thin flat liquid jet).

Another advantage of the present invention is that due to its small size, footprint, factory size, and high contact area, it has less cost and site impact than traditional systems with the same reaction and cleaning capacity, potentially quality and between units. It is possible that the consistency of the can be kept high.

Some of the other features and advantages of the present invention are described in the following description, some are partially apparent from the description, and some are known in the practice of the present invention. The objects and other advantages of the present invention can be realized and achieved by the structures specifically noted in the description, claims and accompanying drawings.

One embodiment of the present invention relates to a gas-liquid contact module. The gas-liquid contact module includes a liquid inlet, a gas inlet, and a gas outlet. The contact module further includes a nozzle array that communicates with the liquid inlet and the gas inlet. The nozzle array produces a plurality of uniformly spaced flat liquid jets with a shape that minimizes disturbances from the airflow. The gas-liquid separator allows the liquid to pass while substantially blocking the passage of the gas. The liquid outlet communicates with the gas-liquid separator.

Another embodiment of the present invention relates to a method of treating gas phase molecules with a gas-liquid contactor. The method comprises forming a plurality of essentially planar liquid jets, each comprising a planar liquid sheet, each of which is configured on a substantially parallel plane. In addition, the method involves the step of supplying a gas containing at least one reactive or soluble gas phase molecule and the interaction of at least a portion of the gas phase molecule by mass transfer between the gas phase molecule and multiple liquid jets. It is provided with a step of removing or reacting with.

Another embodiment of the present invention relates to a gas-liquid contact system. The gas-liquid contact system includes a reaction chamber, a gas inlet connected to the reaction chamber, a gas outlet, and a liquid plenum. The nozzle array provides a plurality of essentially planar liquid jets connected to a liquid plenum, each containing a planar liquid sheet, each configured on a substantially parallel plane. The system also includes a gas-fluid separator connected to the reaction chamber.

Another embodiment of the present invention relates to a gas-liquid contactor. The gas-liquid contactor includes a fluid plenum that supplies the contact liquid and a contact chamber that communicates with the fluid plenum and receives the contact liquid from the fluid plenum. The gas inlet and outlet communicate with the contact chamber. The gas-liquid contactor system takes about 5 seconds^-1About 250 seconds from^-1The interaction is performed by mass transfer having a volume mass transfer coefficient in the range of.

Yet another embodiment of the present invention relates to a gas phase molecular treatment system. The gas phase molecular processing system includes a plurality of modular gas-liquid contactors arranged in parallel or in series so that they can be sized according to the gas phase molecular processing.

Another embodiment of the present invention relates to a gas-liquid contact system that improves the performance of a gas-liquid reactor by utilizing a flat jet having an improved specific surface area (for example, a thin flat liquid jet). In this embodiment, a rigid nozzle plate is utilized that includes a plurality of orifices that produce a very thin flat jet. The flat jet orifice, in one configuration, includes a V-shaped chamber attached to a liquid reagent source. The flat jet orifice may include a pair of opposing planar walls attached to the apex of the V-shaped chamber. The flat jet nozzle may include a conical nozzle mounted as a V-shaped chamber at the opposite end of the opposing planar wall. In another configuration, the jet orifice may include a circular orifice mounted in the liquid source chamber. The flat jet nozzle may generate an oval orifice by including a V-shaped groove that intersects the circular orifice. The orifice of the flat jet may be in a direction perpendicular to, opposed to, or parallel to the gas source inlet. The minimum passage of the flat jet nozzle may be larger than about 250 μm. The nozzle may produce a liquid flat jet whose width is at least 10 times greater than its thickness. Flat jets can be as thin as 10 μm or less, separated at intervals greater than or less than 1 mm, with high packed jet density (β = 0.01) and large specific surface area (approximately 20 cm).^-1) Can be achieved. This is a significant improvement of about 5 to about 10 times over the specific surface area values found in Table 1. The thin jet exposes more liquid to the airflow, resulting in a higher yield of reaction products to the flow of unit liquid mass than conventional contactors.

Another embodiment of the present invention has an orifice having a large specific surface area, a uniform jet velocity, a shape capable of minimizing gas disturbance of a liquid jet, and no salt damage or clogging. The present invention relates to providing a gas-liquid contactor that produces a plurality of densely spaced, thin flat jet streams operating within gas processing streams of cross-flow, parallel-flow, back-flow, and parallel-flow.

Another embodiment of the present invention relates to improved COIL. The COIL includes an excited oxygen generation chamber with an inlet for the chlorine source and a flat jet nozzle for the BHP source. The nozzle has a minimum dimension of length greater than about 600 μm and produces a thin flat jet with a large specific surface area. The photon production chamber has a passage connected to an excitation oxygen generation chamber and an inlet for iodine. The BHP orifice may produce a flat jet of basic hydrogen peroxide that is at least 10 times wider than its thickness. The hydrogen peroxide source may be basic hydrogen peroxide utilizing a single base or a plurality of bases. The single base may be potassium hydroxide or any alkali hydroxide. The nozzle may have a pair of parallel and opposing plates with a second end attached to the conical nozzle. The nozzle may have a pair of V-shaped plates connected to the first end of a pair of parallel and opposing plates.

Another embodiment of the invention has an inlet for a hydrogen peroxide source and a flat jet nozzle for alkaline (Li, Na, K) and alkaline earth (Mg, Ca) hypochlorite sources. It relates to improved COIL including an excited oxygen generation chamber. The hydrogen peroxide of this embodiment is a gas. The nozzle has a minimum dimension of length greater than about 600 μM and produces a thin flat jet with a large specific surface area. The photon production chamber has a passage connected to an excitation oxygen generation chamber and an inlet for iodine.

Another embodiment of the present invention is oxygen, CO.₂, Other nutrients or feed gases, and improved fermentation reactors including nozzles containing multiple orifices to produce flat jets of fermentation medium.

Another embodiment of the invention provides a flat jet generator with a large specific surface area for use in a gas cleaning process that separates ammonia, carbon dioxide, acid gas, hydrogen sulfide, or sulfur dioxide from the gas by liquid contact.

Another embodiment of the present invention provides a large specific surface area injection device utilized in a gas-liquid jet combustion engine.

Yet another embodiment relates to a high performance gas-liquid contactor. The gas-liquid contactor includes a fluid plenum that supplies the contact liquid. The gas-liquid contactor further includes a contact chamber that communicates with the fluid plenum to receive the contact liquid from the fluid plenum. The gas-liquid contactor further includes a gas inlet that communicates with the contact chamber to supply the gas and a gas outlet that communicates with the contact chamber to carry the gas to the outside. Furthermore, the gas-liquid contactor is about 1 cm.^-1About 50 cm from^-1It is characterized by a specific surface area in the range between, and a pressure drop of less than about 5 Torr.

Another feature is that the specific surface area is about 10 cm.^-1About 20 cm from^-1It may be in the range between. The pressure drop of the gas-liquid contactor of the present embodiment ranges from about 5 Torr to about 10 Torr. One feature of the embodiment is that the airflow volume of the reactor at the coal combustion power plant output passing through the reactor with a volume of less than about 15 cubic feet is per minute and per mol weight (MW) of the plant output. Larger than the actual approximately 2500 cubic feet, or the ratio of gas flow to the volume of the reaction chamber is 100 minutes^-1From 1000 minutes^-1There is something that is in the range of. Another feature is that the liquid driving pressure that places the contact liquid in the contact chamber is low (eg, less than 50 pounds per square inch (psi)). Another feature is that the liquid drive pressure is less than about 20 pounds per square inch (psi). Another feature is that liquid contamination is eliminated by about 99%. Another feature is that the contact liquid is arranged by a plurality of nozzles that generate a flat liquid jet, and the plurality of nozzles are arranged so that the jets generate a row of a plurality of parallel jets. There is something. Another feature is that the gas flows through the contact chamber parallel to the row of jets.

Another embodiment of the present invention relates to a method of bringing a gas into contact with a liquid. The method comprises providing a gas-liquid contactor containing a fluid plenum that supplies the contact liquid, and providing a contact chamber that communicates with the fluid plenum and receives the contact liquid from the fluid plenum. The contact chamber includes a gas inlet that communicates with the contact chamber to provide gas and a gas outlet that communicates with the contact chamber to carry gas to the outside. Gas-liquid contactor is about 1 cm^-1About 50 cm from^-1Characterized by a specific surface area in the range between. The gas is driven with a pressure drop of less than about 0.05 psi for one linear foot of airflow in the contactor.

Another feature is that the specific surface area is about 10 cm.^-1About 20 cm from^-1There is something that is in the range between. Another feature relates to the method of driving the contact liquid into the contact chamber at a pressure of less than about 20 pounds per square inch. Another feature is that liquid contamination is eliminated by about 99%. Another feature is that the contact liquid is placed by multiple nozzles that produce a flat liquid jet, and the nozzles are arranged so that the nozzles generate multiple rows of parallel jets. There is. Another feature is that the gas flows through the contact chamber parallel to the sheet of jet.

Another embodiment of the invention relates to a gas-liquid contactor that essentially comprises a plurality of planar liquid jets, each of which comprises a planar liquid sheet and these plurality of liquids. The jets are arranged on parallel planes. A contact chamber containing a plurality of planar liquid jets has inputs and outputs that define the flow of gas. One feature is that the thickness of the flat sheet ranges from about 10 μm to about 1000 μm. As another feature, the thickness may range from about 10 μm to about 100 μm. As another feature, the thickness may be in the range of about 10 μm to about 50 μm. Another feature is that each of the planar liquid sheets is separated from the adjacent planar sheet by a distance of 10 μm or more in a single row and less than about 2 cm between adjacent nozzle rows. There is. Another feature is that the gas-liquid contactor contains multiple nozzles that produce multiple liquid jets, but other geometric configurations are also available. Another feature is that each of the plurality of nozzles has a substantially elliptical outlet. As another feature, a plurality of nozzles may be arranged on one plate. As another feature, a plurality of nozzles may be arranged on the plate so that the gas flows parallel to the flat surface of the flat liquid jet. As another feature, multiple nozzles may be arranged as multiple rows forming a nozzle array and liquid jet. As another feature, the gas-liquid contact module may include an anti-splash grid. As another feature, the members of the anti-splash grid may be angled to aid the flow of liquid after passing through the contact chamber. As another feature, the gas-liquid contact module may include a demister.

Another embodiment of the invention relates to a nozzle that produces a flat liquid jet, which may include a plate containing the nozzle. The embodiment further includes a fluid inlet hole for a nozzle having a V-shaped cross section and a fluid outlet hole for a nozzle having a conical cross section. One feature is that the narrowest hole in the fluid outlet hole engages with the narrowest hole in the fluid outlet hole to form the narrowest hole in the nozzle. As another feature, the narrowest hole in the nozzle may be larger than about 600 μm. As another feature, the base of the fluid outlet hole may be substantially oval.

Yet another embodiment of the invention relates to a plurality of nozzles that include substantially V-shaped channels and produce a thin flat liquid jet that forms fluid inlet holes for the plurality of nozzles. The embodiment further comprises a plurality of fluid outlet holes in the channel, the fluid outlet holes having a conical cross section. As another feature, the plurality of fluid outlet holes may be elliptical. One feature is that the conical cross section and the narrowest hole of the nozzles may be larger than 600 μm.

Another embodiment of this embodiment relates to an exhaust treatment system that includes a plurality of nozzle plates for spraying a solvent. Each of the plurality of nozzle plates has a plurality of nozzles. The present invention further includes a cleaning unit that cleans the combustion exhaust gas and accommodates a plurality of nozzle plates. As one feature, multiple nozzles may produce an array of flat liquid jets. As another feature, a plurality of flat liquid jets may be parallel to the flow of flue gas. As another feature, a plurality of flat liquid jets may be arranged in rows. As another feature, the system may be equipped with a combustion exhaust gas cooler. As another feature, the system may include a combustion exhaust heater. As another feature, the system may include a second cleaning unit. As another feature, the cleaning unit may include a gas-liquid fluid separator. As another feature, the system may include a solvent pump that pumps the solvent into a cleaning unit and multiple nozzles. As another feature, the system may include a solvent capture tank that collects the solvent that has passed through the cleaning unit. As another feature, a plurality of nozzle plates may be removable from the cleaning unit.

Another embodiment of the present invention relates to an exhaust treatment system comprising a plurality of nozzles for spraying a solvent. The embodiment further includes a cleaning unit that cleans the flue gas and accommodates a plurality of nozzle plates. As one feature, multiple nozzles may generate a flat liquid jet. As another feature, multiple flat liquid jets may be parallel to the flow of gas. As another feature, a plurality of flat liquid jets may be arranged in rows.

Another embodiment of the present invention relates to a method of bringing a liquid into contact with a gas. The method provides a contact chamber that includes a liquid inlet point that forms a plurality of flat liquid jets within the contact chamber and forms a flow of gas parallel to the plurality of flat liquid jets. One feature is that the liquid entry point includes a plate that accommodates multiple nozzles. As another feature, the plurality of nozzles may include a fluid inlet hole having a U-shaped cross section and a fluid outlet hole of a nozzle having a conical cross section outlet. As another feature, the method may further configure multiple liquid jets as multiple rows.

Another embodiment of the present invention includes a fluid plenum that supplies a contact liquid, a contact chamber that communicates with the fluid plenum to receive the contact liquid from the fluid plenum, and a gas inlet that communicates with the contact chamber to supply a gas. The present invention relates to a gas-liquid contact device having a gas outlet that communicates with a contact chamber and carries a gas to the outside. The specific surface area of the contact chamber is about 10 cm.^-1About 20 cm from^-1The volume mass transfer coefficient on the liquid side of the contact chamber is greater than about 0.02 cm / s. One feature is that the mass transfer coefficient on the liquid side is greater than about 0.1 cm / s. As another feature, the mass transfer coefficient on the liquid side is greater than about 1 cm / s. As another feature, the mass transfer coefficient on the liquid side is greater than about 10 cm / s. As another feature, the mass transfer coefficient on the liquid side is greater than about 25 cm / s. Another feature is that the mass transfer coefficient on the liquid side is about 50 cm / s or less.

In another embodiment, the fluid plenum that supplies the contact liquid, the contact chamber that communicates with the fluid plenum to receive the contact liquid from the fluid plenum, the gas inlet that communicates with the contact chamber and supplies the gas, and the contact chamber. The present invention relates to a gas-liquid contact device having a gas outlet that communicates and carries a gas to the outside. Specific surface area is about 10 cm^-1About 20 cm from^-1The volume mass transfer coefficient is greater than about 0.2 cm / s. As one feature, the volume mass transfer coefficient is greater than about 1 second-1. As another feature, the volume mass transfer coefficient is greater than about 10 seconds-1. As another feature, the volume mass transfer coefficient is greater than about 100 seconds-1. As another feature, the volume mass transfer coefficient is greater than about 1000 seconds-1. As another feature, the volume mass transfer coefficient is less than about 2500 seconds-1.

Yet another embodiment relates to a gas-liquid contactor comprising a fluid plenum that supplies the contact liquid. The contactor further includes a fluid plenum that produces multiple flat liquid jets and multiple nozzles for fluid communication. The contactor includes a chamber that communicates with the fluid plenum and receives the contact liquid from the fluid plenum through multiple nozzles. The gas inlet communicates with the contact chamber to supply the gas, and the gas outlet communicates with the contact chamber to carry the gas to the outside. One feature is that the ratio of jet length to jet width is about 10: 1. Another feature is that the ratio of jet length to jet width is greater than about 8: 1 and less than about 12: 1. Another feature is that the ratio of jet length to jet width is greater than about 10: 1. As another feature, each of the plurality of flat liquid jets has a thickness of about 10 μm to about 100 μm. As another feature, the length of the jet in each of the plurality of flat liquid jets is generally greater than about 5 cm and less than about 30 cm. Another feature is that the jet speed of multiple flat liquid jets is about 10 m / s.

Yet another embodiment relates to a high performance gas-liquid contactor. The gas-liquid contactor includes a fluid plenum that supplies the contact liquid. The contactor includes a contact chamber that communicates with the fluid plenum and receives the contact liquid from the fluid plenum. The gas inlet communicates with the contact chamber to supply the gas, and the gas outlet communicates with the contact chamber to carry the gas to the outside. Gas-liquid contactor is about 1 cm^-1About 50 cm from^-1It is characterized by an improved specific surface area in the range between, and a very low pressure drop of less than about 5 Torr (or 1 psig). Another feature is that this very low pressure drop is less than about 0.05 psi for the contact distance of the linear gas-liquid contactor. Another feature is that this very low pressure drop is less than about 1 psi for the entire gas-liquid contact system, including the gas heater, gas cooler, and demister. Another feature is that the contact liquid is placed by multiple nozzles that produce a flat liquid jet as the liquid flows through multiple nozzles, the multiple nozzles being placed so that multiple parallel jet rows are formed. Has been done. Another feature is that the gas flows through the contact chamber parallel to the row of jets.

Another embodiment relates to a high performance gas-liquid contactor. The gas-liquid contactor includes a fluid plenum that supplies the contact liquid. The gas-liquid contactor includes a contact chamber that communicates with the fluid plenum to receive the contact liquid from the fluid plenum. The gas inlet communicates with the contact chamber to supply the gas, and the gas outlet communicates with the contact chamber to carry the gas to the outside. Gas-liquid contactor is about 1 cm^-1About 50 cm from^-1Characterized by an improved specific surface area of the range between, the liquid driving pressure to place the contact liquid in the contact chamber is less than about 15 psi. One feature is that the liquid driving pressure for placing the contact liquid in the contact chamber is 10 psi. Another feature is that the contact liquid is placed by multiple nozzles that produce a flat liquid jet as the liquid flows through multiple nozzles, which nozzles are placed such that the jets form a row of multiple jets. Has been done. Another feature is that the gas flows through the contact chamber parallel to the row of jets.

Another embodiment of the present invention relates to a high performance gas-liquid contact module. The module includes a fluid plenum that supplies the contact liquid and a contact chamber that communicates with the fluid plenum and receives the contact liquid from the fluid plenum. The gas inlet communicates with the contact chamber to supply the gas, and the gas outlet communicates with the contact chamber to carry the gas to the outside. Gas-liquid contactors are characterized by a percentage removal rate of more than about 80%. One feature is that the contactor volume is less than about 0.5 m3. Another feature is that the pollutant removal rate exceeds about 90% as a percentage. Another feature is that the pollutant removal rate exceeds about 95% as a percentage. Another feature is that the pollutant removal rate is about 99% percentage. Another feature is the design of multiple modular gas-liquid contactors that can be placed in parallel to make the integrated system as large as needed. Another feature is that multiple modular gas-liquid contactors are arranged vertically. Another feature is that a plurality of modular gas-liquid contactors are arranged horizontally. Another feature is that a plurality of modular gas-liquid contactors are arranged in series. Another feature is that the parasitic load on the system may be less than about 5%. Another feature is that the parasitic load on the system may be less than about 1%. Another feature is SO₂The cleaning and removal rate of pollutants such as, etc. may be greater than about 90% as a percentage. Another feature is SO₂The cleaning and removal rate of pollutants such as, etc. may be greater than about 95% as a percentage. Another feature is SO₂The cleaning and removal rate of pollutants such as, etc. may be greater than about 99% as a percentage.

Yet another embodiment relates to a gas-liquid contact module that includes a plurality of combined features. The module includes a liquid inlet that provides the contact module with a liquid that is reactive or capable of dissolving. In addition, it includes gas inlets and outlets that provide conduits for the contact module to pass through reactive gases or gas solutes or gas phase reactants. The fluid is supplied through the contactor by a nozzle array that communicates the liquid to the liquid inlet, and the nozzle array is uniformly spaced with a shape that can minimize disturbance from the gas flowing through the contactor. Generate multiple flat liquid jets. A gas-liquid separator is arranged so as to cross the contactor chamber from these liquid jet nozzles to allow the liquid to pass while substantially blocking the passage of the gas, which is in liquid contact with the liquid outlet.

Another embodiment of the present invention relates to a method of treating gas phase molecules with a gas-liquid contactor. The method comprises a plurality of basically planar liquid jets, each comprising a planar liquid sheet. The liquid jets are configured on planes that are substantially parallel to each other. The method further supplies a gas containing at least one reactive or soluble gas phase molecule, in which at least one of the gas phase molecules is due to mass transfer interaction between the gas phase molecule and multiple liquid jets. The part is removed.

Yet another embodiment of the invention relates to a gas phase contact system that includes a plurality of combined subsystems. These combined subsystems include a reaction chamber, a gas inlet connected to the reaction chamber, a gas outlet connected to the reaction chamber, a liquid plenum connected to the reaction chamber, a nozzle array connected to the liquid plenum, and Includes a gas-fluid separator connected to the reaction chamber. The nozzle array provides a essentially planar liquid jet. Further, each liquid jet comprises a planar liquid sheet, each of which is arranged as a plurality of liquid jets that are essentially arranged in substantially parallel planes.

Another embodiment of the invention relates to a gas-liquid contactor in which a fluid plenum supplies a contact liquid to a contact chamber. The second feature is that the contact chamber communicates with the fluid plenum and itself receives the contact liquid from the fluid plenum. The third feature is that the contactor has a gas inlet and a gas outlet that communicate with the contact chamber. Overall, the gas-liquid contact system takes about 1 second^-1About 250 seconds from^-1The interaction is performed by mass transfer having a volume mass transfer coefficient in the range of.

It should be understood that the above outline and the following detailed description are exemplary and explanatory and are intended to provide further description of the claimed invention.

The accompanying drawings are included to provide a further understanding of the invention and are included as part of this specification, which constitute the embodiments, illustrates embodiments of the invention, and describes the principles of the invention with description. Play a role.

The following is a brief description of the drawings.

<figref num="1">It is a block diagram of the system which generates a flat jet in one Embodiment of this invention.</figref>

<figref num="2">It is a block diagram of the system which generates the excitation oxygen in another embodiment of this invention.</figref>

<figref num="3">It is a block diagram of the improved chemical oxygen iodine laser in another embodiment of the present invention.</figref>

<figref num="4">It is a top right perspective view of the flat jet nozzle in another embodiment of the present invention.</figref>

<figref num="5">It is the bottom left side perspective view of the flat jet nozzle of FIG.</figref>

<figref num="6">It is a cross-sectional view of the precursor of the nozzle bank in another embodiment of this invention.</figref>

<figref num="7">It is a side view of the precursor of the nozzle bank shown in FIG.</figref>

<figref num="8">It is a top view of the nozzle bank in another embodiment of this invention.</figref>

<figref num="9">It is a side view of the nozzle bank of FIG.</figref>

<figref num="10">It is a cross-sectional view of the nozzle bank of FIG. 8 cut by B of FIG.</figref>

<figref num="11">It is a figure which shows the nozzle bank of FIG. 8 defined by the cutting in A of FIG. 9 in detail.</figref>

<figref num="12">It is a perspective view of the nozzle bank of FIG.</figref>

<figref num="13">It is a perspective view of the plate which welds a nozzle bank.</figref>

<figref num="14">It is a side view of the nozzle plate in another embodiment of this invention.</figref>

<figref num="15">It is a top view of the nozzle plate of FIG.</figref>

<figref num="16">It is a perspective view of the nozzle plate of FIG.</figref>

<figref num="17">It is a detailed exploded view of the nozzle plate of FIG. 14 cut by A shown in FIG.</figref>

<figref num="18">FIG. 3 is a perspective view of an array of flat, thin flat liquid jets produced by the nozzle plate of FIG.</figref>

<figref num="19">FIG. 4 is a front view of an array of flat, thin flat liquid jets produced by the nozzle plate of FIG.</figref>

<figref num="20">FIG. 4 is a side view of an array of flat, thin flat liquid jets produced by the nozzle plate of FIG.</figref>

<figref num="21">The outlet side of the fluid of the nozzle plate in another embodiment of the present invention is shown.</figref>

<figref num="22">The inlet side of the fluid of the nozzle plate of FIG. 21 is shown.</figref>

<figref num="23">The outlet side of the fluid of the nozzle plate of another embodiment of the present invention is shown.</figref>

<figref num="24">The inlet side of the fluid of the nozzle plate of FIG. 23 is shown.</figref>

<figref num="25">The outlet side of the fluid of the nozzle plate from which the nozzle bank has been removed is shown.</figref>

<figref num="26">The inlet side of the fluid of the nozzle plate of FIG. 25 is shown.</figref>

<figref num="27">It is a top view of the precursor of a nozzle bank.</figref>

<figref num="28">It is a side view of the precursor of FIG. 27.</figref>

<figref num="29">It is a schematic cut-out view of the gas-liquid contactor in another embodiment of the present invention.</figref>

<figref num="30">The schematic arrangement of a plurality of gas-liquid contactors in another embodiment of the present invention is shown.</figref>

<figref num="31">FIG. 6 is a schematic diagram of a plurality of pollutant removal systems according to another embodiment of the present invention.</figref>

<figref num="32">FIG. 6 is a schematic diagram of a plurality of pollutant removal systems according to another embodiment of the present invention.</figref>

<figref num="33">It is a schematic diagram of a general gas-liquid contactor that causes an interaction between a gas phase and a liquid phase in another embodiment of the present invention.</figref>

<figref num="34">NO₂It is a graph which shows the relationship between the absorption degree of the removal system and the runtime.</figref>

<figref num="35">CO that turns on / off the jet of liquid ammonia water₂It is a graph of the FTIR (Fourier transform infrared spectrophotometer) absorption spectrum.</figref>

<figref num="36">The 2MW prototype system is shown.</figref>

<figref num="37">Indicates a gas-liquid contactor.</figref>

<figref num="38">The solvent pump of the system of FIG. 41 is shown.</figref>

<figref num="39">H₂SO by 0.13MW scale using O, NaOH (0.1% by weight)₂It is a graph which shows the cleaning result of.</figref>

<figref num="40">CO on a 0.13 MW scale using 19% by weight ammonia water₂It is a graph which shows the cleaning result of.</figref>

<figref num="41">H₂SO by 2MW scale using O, NaOH (0.1% by weight)₂It is a graph which shows the cleaning result of.</figref>

<figref num="42">Represents a 60 MW cleaning unit and support structure.</figref>

<figref num="43">It is a front view of one section of the 2MW section of the scrubber of FIG. 42.</figref>

<figref num="44">It is a side view of one section of the 2MW section of the scrubber of FIG. 42.</figref>

<figref num="45">The layout of the inlet channel and jet filling zone is shown.</figref>

<figref num="46">Represents a jet filling zone with a removable nozzle plate.</figref>

<figref num="47">The configuration of the nozzle plate of the jet filling zone of FIG. 46 is shown.</figref>

<figref num="48">The sealing system of the jet filling zone of FIG. 46 is shown.</figref>

<figref num="49">It is a process flow diagram of the pollutant removal system in another embodiment of this invention.</figref>

<figref num="50">It is a process flow diagram from a pollutant removal system in another embodiment.</figref>

The present invention relates to gas-liquid contactors and exhaust cleaning systems and methods, and more particularly to nozzle arrays that produce a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbances from the gas. Related. In addition, various embodiments provide a plurality of small, single-unit processes integrated into a module, and these designs overcome the shortcomings of conventional designs. Modularizing single-unit processing allows you to scale small systems to accommodate the scale of processing by simply multiplying the module by a convenient integer.

In addition, a single gas-liquid contactor capable of producing a thin flat liquid jet can be multiplied and integrated into one or more modules that are done within the airflow rate of the design, which is very small. Is much smaller than conventional backflow reactors in terms of yield of homogeneous reactors. Integration into one or more modules may be done in series or in parallel.

In a series embodiment, the modules are combined one by one with the gas flowing through each module in sequence. Of course, some modules have loops that are bypassed or recirculated. In addition, the module may be performed in the same liquid phase or in different liquid phases, depending on the desired selectivity of the reaction of interest for capture and sequencing of gas molecules.

In a parallel embodiment, the modules are included next to or on top of each other so that all processing or cleaning of the same gas supply takes place, and where each module is substantially equal to the adjacent module. Try to process by molecular weight. In general, parallel modules perform operations in the same liquid phase as each other because the processing for each is performed at the same time as that of the adjacent module.

One embodiment of the present invention aims to accommodate higher airflow rates or lower mass transfer coefficients than the design standard for this single module, the module itself being multiplied by a convenient integer unit and the subject process. Can be a larger functional module with longer contact times without splitting the form into multiple overlapping systems. In addition, this design logic may be extended to other submodules of the chemical processor (eg, liquid capture and liquid delivery systems), all of which correspond to a single airflow mainstream plenum and a single liquid processing stage. ing. Capital-intensive equipment (eg pumps and blowers from airflow and / or liquid flow systems) can be linearly scaled to supply increased modules, and the unique designs of these modules are coupled together. This forms a functionally single process in a very small design.

In another embodiment of the invention, the module can force a very high rate of liquid phase by utilizing a liquid jet (eg, a thin flat jet), which causes mass transfer of gravity. Or eliminate the dependence on buoyancy. The liquid can flow at a very high rate, and the gas phase can flow very fast along the same vector, or in the opposite direction of the flow, and also in the lateral direction. Since all flows are fast, the direction of flow can be chosen for design reasons rather than being constrained by gravity or thermal convection. In addition, the mass transfer and volume transfer coefficients are very high, and the length of contact can again be modularly scaled to accommodate both loading and reaction yields.

In another embodiment of the invention, the gas-liquid contactor selectively fills a gas reactant with a high mass transfer rate, from a high volume of gas flow rate, to a continuously filled gas constrained by a small system volume. Is configured to reach the flow velocity of. In addition, various methods of the invention allow a large, densely packed, fast, stable liquid jet (eg, a thin flat liquid jet) to interact with a high speed air stream. The orifices and densities that form the jet can be optimized based on the liquid solvent or reaction characteristics such as viscosity and surface tension. In general, increasing liquid viscosity also improves the stability of the liquid jet, if chamber size or the entire processing scale is not taken into account. Therefore, the nozzle density of the nozzle array increases as the nozzle size decreases. This is not required, but may be desirable for the purposes of reducing jet-to-jet spacing and increasing and optimizing the specific surface area of the contactor. In contrast, low surface energies tend to destabilize the jet, leading to the formation of small droplets under some conditions, which is not desirable in the present invention but is commonly seen at current state of the art. Be done. For low surface energies, it may be possible to optimize jet properties for any fluid by lowering the hydraulic pressure and increasing the nozzle size.

In one embodiment of the invention, the efficiency of treating gaseous and liquid reactants is increased as compared to conventional methods and systems. The efficiency of the method and system is achieved by low pressure solvent treatment requiring minimal pumping function in the system due to the large mass transfer coefficient and the resulting small size, low tolerance of the liquid jet and the modularized combined nature of the design. Thus, embodiments of the present invention achieve unexpected results, one example of which is a foot that is at least 10 times smaller than a conventional reactor at a cost of capital that is at least less than half that of a conventional gas-liquid contactor. Printable and substantially uniform performance is achieved.

One embodiment of the present invention relates to a gas-liquid contact module. The gas-liquid contact module includes a liquid inlet and outlet, as well as a gas inlet and outlet. The module also includes a nozzle array that communicates with a liquid inlet and a gas inlet, which produces a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbances from the gas. The module also includes a gas-liquid separator that allows the passage of liquid and at the same time prevents the passage of gas. Modules can be connected in series and in parallel with other modules.

Modules can be manufactured from a number of different materials (eg, copper, nickel, chromium, steel, aluminum, coated metals, and combinations thereof). In addition, the module may include at least one of a plastic material or structural polymer, polyimide, a compound thereof, or a combination thereof.

The nozzle array can be formed in a plurality of different configurations (eg, staggered configurations). In one staggered configuration, the first, second, and third nozzle rows are offset between the first and third nozzle rows, with the second nozzle row offset. It is configured to be located.

The nozzle array may further include a plurality of nozzles at predetermined intervals. Nozzles may include at least two nozzles separated by a distance greater than about 0.2 cm. The nozzle may contain any number of rows and columns. In a preferred embodiment, at least three nozzle rows are arranged and separated at a uniform distance. The distance between the nozzles ranges from about 0.1 cm to about 5.0 cm.

The nozzle may be formed from liquid channels having a plurality of different geometric shapes (eg, U-shaped channels, V-shaped channels, etc.). Channels can be formed using a variety of methods (methods include machining or forming metal, compound, ceramic plates, or machining nozzle orifices into tubular or partial shapes of tubes. Including, but not limited to these). When machining a single plate, U or U-shaped channels are machined to the liquid side of the plate. The processing side of the plate of these channels is then branched by a second V-shaped groove, the depth of which penetrates the liquid channel space. Depending on the depth of the second groove, the size of the hole or nozzle formed at the intersection between the liquid channel and the channel on the processing side will vary.

The higher the level of penetration at an intersection, the larger nozzles are formed. That is, large nozzles are generated depending on the amount of V or U-shaped channels at the intersection of the cones. When forming a tubular nozzle, the tangent cutting point is formed at an angle of approximately 90 degrees to the axis of the radius of the tube (on the processing side) outside the radius. The liquid channel that supplies the nozzle has a depth of more than about 2 mm. In embodiments of the invention, the channel depth may range from about 2 mm to about 20 mm.

In another embodiment, the shape of the nozzle may be a substantially elliptical shape in which the ratio between the major axis and the minor axis is less than 0.5. In other embodiments, the nozzle is about 0.25 mm.²From about 20mm²It may have a projected cross-sectional area in the range of. The projected cross-sectional area is determined by the elevation of the position of the two-dimensional shape of the nozzle projected onto the two-dimensional surface with the back cooler, but the actual shape is determined by both the depth and radius of the cut point. It goes without saying that it becomes three-dimensional and complicated based on the shape of the curvature of the channel and / or.

Another embodiment of the present invention relates to a method of treating gas phase molecules with a gas-liquid contactor. The method comprises forming a plurality of substantially planar liquid jets, each of which is formed on a planar liquid sheet. The plurality of liquid jets are arranged in a plane substantially parallel to each other. The method further provides a gas with at least one reactive or soluble gas phase molecule.

In this embodiment, at least a part of the gas phase molecule is removed by the interrelationship regarding mass transfer between the gas phase molecule and the liquid jet. Gas phase molecules are, for example, industrial emissions from coal-fired power plants or other industrial emissions such as pollutants, pollutants (eg SO)._x, NO_x, CO₂, Hg) and combinations thereof. Of course, HCl, HBr, HF, H₂SO₄, HNO₃Acid gas, CO, H, etc.₂Other gas molecules such as S, amines (including ammonia), alkanolamines, ureas, formamides, alcohols, carboxylates (such as acetic acid), combinations thereof and a wide variety of other gas phase molecules can also be removed. The limitation of the present invention is only the function of providing a gas phase molecular reactant or solute, and a liquid phase in a range that is reactive or soluble. Although the main description of the specification of the present invention is intended for an aqueous solution system, those skilled in the art can easily understand that the invention of a serious liquid contactor can be applied to a non-aqueous solution system. For example, partial fluorination of pharmaceutical products or chlorination of raw materials for petrochemical products is known.

In one embodiment of the invention, the liquid may be selected to remove contaminants contained in known gases. The basal aqueous solution is SO₂It may be used to remove other combustion emissions constituents (eg, about 0.1M to about 1.0 NaOH, NH).₄HCO₃, Na₂SO₃And so on). As is known, the concentration of these liquid reactants can be adjusted depending on the mass transfer of gas-liquid interactions and suitable products.

In addition, some examples of liquids include water, ammonia, ammonium salts, amines, alkanolamines, alkaline salts, alkaline earth salts, peroxides, hypochlorite hydrochloride, calcium salts, magnesium, and combinations thereof. At least one of these aqueous solutions may be included. Other aqueous solutions may include seawater, salt water, combinations thereof and the like.

Seawater or saltwater is SO based on pH control and other technical factors₂Or CO₂, Or both are available when cleaning. In addition, these liquids are also effective in cleaning other acid gases such as HCl or HF.

At least one jet is formed by the method. The jet may have various physical dimensions. For example, the jet may have a length in the range of 5 cm and 20 cm, a jet width of 1 cm to 15 cm, and a jet thickness of between 10 μm and 1000 μm. In addition, the length-to-width ratio of the jet may range from 0.3 to 20.

As another embodiment of the present invention, a gas-liquid contact system including a plurality of combined subsystems is provided. These combined subsystems include a reaction chamber, a gas inlet connected to the reaction chamber, a gas outlet connected to the reaction chamber, a liquid plenum connected to the reaction chamber, a nozzle array connected to the liquid plenum, and a nozzle array. Includes a gas-liquid separator connected to the reaction chamber. With respect to the nozzle array, the nozzle array is configured to provide a substantially planar liquid jet. Further, each liquid jet includes a flat liquid sheet, and the plurality of liquid jets are arranged so as to be present in planes substantially parallel to each other.

Embodiments of the present invention will be described in detail below, and examples thereof are shown in the accompanying drawings.

FIG. 1 is a block diagram of a system for generating a flat jet according to an embodiment of the present invention. Referring to FIG. 1, system 0 includes a flat jet orifice array for producing high density, high surface area liquid jets (eg, thin flat liquid jets). In this embodiment, a small segment of the nozzle array is machined from a single plate. This shows a V-shaped liquid channel, but in this example, the treatment-side orifice intersects the V-liquid channel with a cone on the opposite side of the groove. However, the resulting nozzle orifice is still oval. The orifices included in the nozzle array are staggered so that they are separated from each other. This distance ranges from about 0.1 cm to about 5 cm in the x direction and may be about 2 mm in the y direction. In a preferred embodiment, this distance is 2 cm in the x direction and 2 mm in the y direction. Of course, the distance between the orifices does not have to be constant across the orifice array.

The orifice has a V-shaped inlet 1 and two conical outlets leading to the jet. An orifice is formed by the interaction of inlet 1 and outlet 2 channels. The cross-sectional view of the nozzle plate 3 shows the contours of the inlet 4 and outlet 5 channels. The outline of the jet exiting the orifice is shown in 7. An enlarged view of the cross section of Inlet 8 and Exit 9 channels is provided. A thin flat liquid jet may be formed of variable length (eg, the ratio of jet length to jet width may be about 10: 1 and the jet may have a thickness in the range of about 10 μm to about 100 μm. ). The jet length may range from about 5 cm to about 20 cm. The jet width may range from about 0.5 cm to about 20 cm.

FIG. 2 is a block diagram of a system that produces excited oxygen according to another embodiment of the present invention. Since COIL utilizes the nozzle array in one embodiment of the present invention having the function of producing a liquid having a large specific area (for example, basic hydrogen peroxide), it is more efficient and lighter than the prior art design. , Small size. In Figure 2, COIL is represented by reference number 10. COIL10 is used to generate excited oxygen. COIL 10 includes a gaseous reactant source 12 (eg, chlorine gas) attached to the manifold 14. The manifold 14 has a plurality of openings such as holes (not shown) for inserting a gas jet into the excited oxygen generation chamber 20. COIL10 is also the source of the liquid reactant 22 (eg, a single base). It has basic hydrogen peroxide) formed by base). In one embodiment, the single base is potassium hydroxide (KOH). The source of basic hydrogen peroxide 22 is connected to a plurality of nozzles 26 by a pipe 224. Nozzle 26 is configured to form a thin flat jet 28 for liquid basic hydrogen peroxide. The thin flat jet 28 for hydrogen peroxide 22 reacts with the jet for chlorine gas to produce excited oxygen 32. COIL10 may further include a method of collecting basic hydrogen peroxide for reuse (eg, a recycling loop).

By using the liquid jet, the specific surface area of hydrogen peroxide 22 is increased, and the reaction efficiency with chlorine gas 12 is increased. Tests have shown that the specific surface area of thin flat liquid jets is more than three times that of circular jets of related technology. In addition to increasing the surface area of hydrogen peroxide, the flat jet does not require the small throat required by prior art nozzles. More specifically, prior art nozzles had throat sizes ranging from about 150 μm to about 350 μm. The nozzle 26 can utilize a throat larger than about 250 μm, and more preferably a throat larger than 600 μm. Therefore, the nozzle 26 is less likely to be clogged with contaminants (eg, salts produced by the reaction of hydrogen peroxide with chlorine gas). In addition, this allows System 10 to utilize a basic hydrogen peroxide solution with a high initial molar concentration (eg, a high molar concentration of about 10 mol / L). Prior art systems generally limited the initial molarity to 5 mol / L due to the clogging of the system with contaminants such as salts. Most systems reuse hydrogen peroxide, but once the molar concentration drops to about 2.5 mol / L, the performance of the system deteriorates significantly. As a result, in most of the prior art systems, the difference in molar concentration was limited to the range of about 2.5 mol / L to about 5 mol / L, but in this embodiment, the difference in molar concentration is about 2.5 mol / L. It can range from L to about 10 mol / L. Therefore, the device can carry 1/3 of the basic hydrogen peroxide of the prior art system and have 3 times the capacity.

In another embodiment, the COIL is an excited oxygen generation chamber with a hydrogen peroxide source inlet and a flat jet nozzle for alkaline sources (Li, Na, K) and alkaline earth (Mg, Ca) hypochlorites. including. Hydrogen peroxide is a gas. The nozzle has a plurality of orifices of the smallest size capable of producing a thin flat jet having a length of more than about 300 μm and a large specific surface area. An excitation oxygen generation chamber and a photon generation chamber with passages connected to the inlet for iodine are provided.

FIG. 3 is a block diagram of an improved chemical oxygen iodine laser in another embodiment of the present invention. In Figure 3, the improved COIL is generally indicated by reference number 50. The COIL 50 has a source 52 of gas (eg, chlorine gas physically connected to the excited oxygen generation chamber 56 via multiple inlets by conduits or pipes 54). The liquid reactant source 58 (eg, basic hydrogen peroxide 58) is transported from the pipe 60 to the flat jet nozzle array 62. The nozzle 62 mixes the liquid basic hydrogen peroxide 58 with the chlorine gas 52. This reaction produces excited oxygen 64, including singlet delta oxygen. Excited oxygen 64 is transported to the photon generation chamber 66. The iodine source 68 is connected to the inlet 70 of the photon production chamber 66. The iodine source 68 disrupts the excited oxygen 64 and emits photons. The photon generation chamber 66 has a mirror that provides the lasing 72 with an output perpendicular to the flow of excited oxygen. The consumed oxygen 74 exits the photon generation chamber 66. Laser 50 may include a system that regenerates basic hydrogen peroxide for reuse purposes. COIL50 utilizes a nozzle array 62 to increase the surface area of hydrogen peroxide and increase the initial molar concentration of basic hydrogen peroxide. As a result, the COIL50 can be more efficient, achieve smaller size and lighter weight than prior art systems, or increase laser emission capacity.

FIG. 4 is a top right perspective view of an embodiment of the flat jet nozzle according to the embodiment of the present invention. In FIG. 4, nozzle 80 has a V-shaped chamber 82 with apex 83 attached to a first end 84 of a pair of opposing plates 86. The second end 88 of the pair of opposing plates 86 is attached to the conical nozzle 90. A liquid (eg, basic hydrogen peroxide) flows into a V-shaped liquid supply channel or chamber 82, forces between a pair of opposing plates 86 and then exits into nozzle 90, a flat liquid jet. Form 94. Depending on the nozzle area, the jet flow rate and velocity, the jet thickness 96 may range from about 5 μm to about 100 μm, and the width 98 may range from 1 cm to about 5 cm.

In this embodiment, the ratio of width to thickness is significantly greater than the coefficient 10. For example, at a jet speed of about 10 m / s, the length of the flat jet stream may be about 15 centimeters or more. The narrowest passage 100 is where the conical nozzle 90 joins the pair of opposing flat plates 86, exceeding about 600 μm. The nozzle 80 increases the surface area of the liquid (eg, basic hydrogen peroxide), which significantly increases the reaction efficiency between the basic hydrogen peroxide and chlorine. Furthermore, due to the large surface area of the jet and the small jet thickness of this nozzle 80, it is approximately 10 cm.^-1About 20 cm from^-1A very large specific surface area is generated, which reduces the volume of the generator and increases the yield of excited oxygen supplied to the laser cavity. In addition, the nozzle 80 does not require a small throat or passage that is prone to clogging with contaminants (eg, salts produced by the reaction of chlorine with basic hydrogen peroxide), so the system has a higher initial molar concentration. Basic hydrogen peroxide can be used.

FIG. 5 is a perspective view of the bottom left side of the flat jet nozzle of FIG. The flat jet nozzle 80 of FIG. 5 includes a plurality of conical nozzles that can be attached to the second end of a pair of opposing flat plates 86. The only outlet from the second end of the pair of opposing flat plates 86 passes through the conical nozzle. Although this description focuses on the use of COIL, it should be noted that these embodiments are applicable to any two-phase reactor or contact system. This two-phase reactor system significantly increases the interaction between gas phase reactants and liquid phase reactants. As a result, the reaction is significantly more efficient than that of the prior art two-phase reactor design.

So far, we have described COIL, which is lighter, smaller, and more efficient than the prior art COIL lasers, which have similar capacities. This allows the laser to be used in smaller transport systems or to increase the capacity of current transport systems.

&lt;Exhaust contact system and method&gt;

As mentioned above, System 0 provides a nozzle array that produces a flat jet that is thin, dense, and has a large surface area. The explanation was given from the point of using system 0 with COIL. In an alternative embodiment, many of the principles of System 0 apply to pollutant mitigation systems and methods. The pollutant mitigation system and method in one embodiment includes a gas-liquid contactor. The gas-liquid contactor includes a plurality of nozzle plates. In this embodiment, each nozzle plate includes a plurality of nozzles shown in FIGS. 6 to 17, and the plurality of nozzles 1010 form a nozzle array.

Regarding pollutant reduction systems and methods, first the nozzle 1010 in the unique invention, then the nozzle plate and the unique nozzle arrangement, the configuration of the gas-liquid reactor, the overall configuration of the pollutant reduction system and method, and finally. An example of system implementation for various pollutants will be described with reference to a bottom-up schematic. It is clear from the description below that the subcomponents of pollutant mitigation systems and methods are available for a number of applications beyond those relating to pollutant mitigation systems and methods.

&lt;Nozzle&gt;

As mentioned above, the orifice that supplies the flat jet of hydrogen peroxide for System 0 will be described. The orifice has a V-shaped inlet 1 and a conical outlet 2 channels for jet forming purposes. The intersection of inlet 1 and outlet 2 channels forms an orifice. The cross-sectional view of the nozzle plate shows the contours of the inlet 3 and outlet 4 channels. An outline of the jet exiting the orifice is shown in 5. An enlarged view of the cross section of the inlet 6 and outlet 7 channels is provided. The ratio of jet length to jet width is about 10: 1 and the thickness ranges from about 10 μm to about 100 μm.

In addition to increasing the surface area of the reactants or sorbents, flat jets do not require the small throat required by the nozzles of related technology. As previously described, the nozzles of the relevant art have throat sizes ranging from about 150 μm to about 350 μm at maximum. In contrast, in embodiments of the present invention, the flat jet nozzle may have a throat that is about 250 μm or larger relative to the size of the small nozzle. For example, a flat jet nozzle may have a throat in the range of about 250 μm to 2000 μm. Therefore, the nozzles of the embodiments of the present invention are less likely to be clogged by contaminants (eg, salts formed by the reaction of a liquid sorbent with a gas), which makes the system of the present invention robust. Become. Furthermore, the initial molar concentration of the reactants may be increased, and even finer solvent slurries can be used. High molar concentrations of about 10 mol / L will be available, but prior art systems generally have an initial molar concentration of about about due to clogging of salt and / or solid by-products or precipitates. It was limited to 5 mol / L. Most systems reuse liquid sorbents or reactants, but once the molar concentration drops significantly, the performance of the system deteriorates significantly. In embodiments of the invention, the liquid of the sorbent or reactant can be easily replenished by simple concentration monitoring and proper titration of the reactant into the liquid system.

The nozzle 1010 shown in FIGS. 8 to 13 is similar to the conical nozzle 90 described above. For example, similarities can show the resulting nozzle cut as the intersection between the approximated cone and the U-shaped channel, though not in a way that utilizes a cone-shaped machining tool bit. Manufactured. Nozzle 1010 has a configuration that produces a flat jet as the liquid flows and produces a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbances from the gas in a gas-liquid contact system. Flat jets with plug flow characteristics can also be produced. The first flat jet produced has very low turbulence characteristics and can maintain the characteristics of the flat jet for a significant length.

FIG. 6 is a cross-sectional view of an embodiment of a nozzle bank precursor. FIG. 7 is a side view of the precursor of the nozzle bank shown in FIG. With reference to FIGS. 6-8, the precursor rod 1012 is utilized to form the nozzle 1010 and the nozzle bank 1011. Rod 1012 has various dimensions and generally resembles the flattened shape of a half pipe. The material of the precursor can take a number of different geometric shapes (eg, oval, oval, semi-circular).

The rod 1012 has a shell rod thickness of 1015, a rod straight height of 1016, and a total rod height of 1017. In embodiments of the invention, the shell rod thickness 1015 may range from about 0.015 inches to about 0.055 inches, and the straight rod height 1016 may range from about 0.05 inches to about 0.75 inches. The total height of the rod 1017 may range from about 0.25 inches to about 0.95 inches. The shell rod thickness 1015 of the rod of the preferred embodiment is about 0.035 inches, the maximum measured value of the rod width 1014 is about 0.323 inches, the linear height 1016 of the rod is about 0.10 inches, and the total height of the rods. The 1017 may be about 0.31 inches and the rod length 1018 may be about 7.470 inches. The overall width 1014 is about 0.323 inches, and the nozzle end 1019 starts about 0.035 inches from the end of the nozzle bank 1011, as shown in FIG.

The procedure for creating the nozzle bank 1011 of this embodiment is as follows. Nozzle bank 1011 is formed using a progressive die. In the first step of cutting the die, a rectangular piece of metal of appropriate size is formed. A single metal or alloy (eg, stainless steel) may be utilized as the material for the die. In addition, the choice of metal can be made depending on the liquid chemicals utilized and their corrosiveness and reactivity, thus other metals including copper, nickel, chromium, aluminum or alloys containing these metals. You can also select.

In the second stage, the specific geometric shapes shown in FIGS. 6 and 7 are formed. It is preferred that the rod 1012 be deburred to eliminate sharp edges or corners. A plurality of nozzles 1010 are then formed by aligning the nozzles 1010 within the rod 1012. In a preferred embodiment, the nozzle 1010 is formed utilizing an electric discharge machine (EDM). For example, rod 1012 is attached to a fixture and placed in a manufacturing EDM to form a nozzle into rod 1012 (see FIGS. 8-11).

In FIG. 12, the end cap 1023 is welded to the nozzle bank 1011 and the nozzle bank 1011 is welded to the plate (see FIG. 13). Welding can be performed by a method known as prior art (eg, laser welding). In FIGS. 8 to 13, nozzle row 1011 is shown as including the completed nozzle 1010. It can be seen from FIG. 11 that the nozzle 1010 is cut at an angle of about 90 degrees. The cutting depth of the nozzle may range from about 1 mm to about 2.5 mm. In a preferred embodiment, the cutting depth 1020 of nozzle 1010 is about 0.058 inches. The channel depth may range from about 2 mm to 20 mm.

These nozzles may be formed so that there is a uniform or non-uniform distance between the centers 1021. In embodiments of the present invention, the distance between the centers may range from about 0.1 cm to about 5 cm. In a preferred embodiment, the distance between the nozzle centers 1021 is about 0.158 inches. In addition, there may be any number of nozzles in the nozzle bank 1011. In a preferred embodiment, the nozzle bank 1011 is formed with 45 nozzles. In addition, end space 1022 is formed at both ends of the nozzle bank 1011. In a preferred embodiment, the end space 1022 is formed to be approximately 0.235 inches. FIG. 12 shows how the nozzle end cap 1023 is welded. FIG. 13 shows the nozzle bank 1011 welded to the plate 1024 along the channel seam 1025. The configuration of this embodiment is advantageous because it can provide a large surface area relative to the volume of the liquid and can provide a large number of jets to a low volume contactor at normal atmospheric pressure. In another embodiment, instead of the welds described, the channel can be machined directly onto the plate. In addition, the nozzle may have a narrow, substantially oval slit (minimum dimension less than about 0.5 mm and length greater than about 50 mm). This nozzle may form an unnecessarily large liquid flow volume as compared to a preferred embodiment, but can form a thin flat liquid sheet with a large surface area.

&lt;Nozzle plate&gt;

By arranging the nozzle 1010 on the nozzle bank 1011 or on the plate 1024, the liquid jet formed by the nozzle is densely filled with a small volume. By making the fluid flow predictable, the jets are densely packed without interference and without forming turbulence. The fluid flow of a preferred embodiment is such that the incoming liquid flow is about 90 degrees with respect to the direction of the liquid nozzle supply channel. It has been found that this produces the best liquid jet properties in the water fluid (ie, in a fluid flow along or parallel to the liquid supply channel, the resulting jet is oriented along the fluid flow. It will be changed and will have a negative effect). In contrast, in the jet laminar flow formed by the nozzle plate 1020, a densely packed jet is produced without the adjacent stream rows intersecting each other. Therefore, almost no turbulence is formed and the fluid is evenly distributed.

FIG. 14 is a side view of the nozzle plate according to another embodiment of the present invention. FIG. 15 is a top view of the nozzle plate of FIG. FIG. 16 is a perspective view of the nozzle plate of FIG. FIG. 17 is a detailed exploded view of the nozzle plate of FIG. 14 cut at A shown in FIG.

With reference to FIGS. 14-17, the nozzle plate is generally indicated by reference number 1020. In this embodiment, each of the individual nozzles 1010 is cut into the formed channel 1015 to form a row of nozzles in the channel 1015. Several channels are formed on the plate 1020 to form an orifice plate or nozzle jet array. As mentioned above, the channel 1015 may be a nozzle bank 1011 welded to a single plate. Alternatively, the channels and nozzles may be formed from a single plate by machining, the results of which are generally as shown in FIGS. 21-24.

In this embodiment, these nozzles 1010 are arranged at precise spacing to maximize the capacity of the generated jets so that the jets meet the intended volume but do not intersect each other. If the distance between the jets is too close, the jets will collide with each other or split into small droplets, and the flat jets will not be in close contact with each other, resulting in an unfavorable result that the effect of the present embodiment is reduced. On the other hand, if the distance between the jets is too large, the specific surface area capable of reacting with the gas phase molecules becomes small, and the effect of the present embodiment is also reduced. Optimal spacing is determined primarily as a function that combines nozzle design and size, reaction effects (or mass transfer), fluid viscosity, and fluid surface energy.

FIG. 18 is a perspective view of an array of flat, thin, flat liquid jets produced by the nozzle plate of FIG. FIG. 19 is a front view of an array of flat, thin, flat liquid jets produced by the nozzle plate of FIG. FIG. 20 is a side view of an array of flat, thin, flat liquid jets produced by the nozzle plate of FIG.

18 to 20 show an array or matrix of flat jets formed when a liquid is swept through a nozzle with strong force. In this embodiment, each nozzle 1010 is configured to form a flat and stable jet 1050. In a preferred embodiment, the jet is formed to be about 2 cm wide, about 25 cm long, and about 0.1 mm thick. Of course, other dimensions can also be used. Rows 1055 of each nozzle form a row of jets 1060, and a plurality of rows side by side form a matrix or array of flat liquid jets 1065. This plate is configured to form a 24-row jet 1055. Of course, the number of lines may be adjusted. The number of suitable jet rows may be determined by the size of the gas-liquid contactor and the practical mode of manufacture of the nozzle array or jet plate and the accompanying fluid processing hardware. However, there is no basic restriction on the size on the upper surface side. For very small reactors (eg, those made to research dimensions), the actual number of rows required to provide two liquid channels is three (and half on the reactor wall). This means that each end will have half of one channel). In operation, the gas is configured to flow between the flat jets parallel to the flat side of the jet, which results in a very large surface area and close contact is achieved.

FIG. 21 shows the outlet side of the fluid in the nozzle plate according to another embodiment of the present invention. FIG. 22 shows the inlet side of the fluid in the nozzle plate of FIG.

With reference to FIGS. 21 and 22, the nozzle plate is generally represented by reference number 1101. The nozzle plate 1101 includes a plurality of offset and staggered nozzles 1010. In one embodiment, as shown in FIG. 18, the gas may be configured to flow parallel to the flat surface produced by the jet. The staggered or offset configuration of nozzle 1010 shields the channels of cross-flow gas rather than turbulence, thus allowing a slight increase in flow compared to non-staggered configurations.

FIG. 23 shows the outlet side of the fluid in the nozzle plate of another embodiment of the present invention. FIG. 24 shows the outlet side of the fluid in the nozzle plate of FIG. 23.

With reference to FIGS. 23 and 24, the nozzle plate is generally designated by reference number 1110. The fluid may exit the plane shown in FIG. 23 and the gas may be configured to flow parallel to the flat surface of the jet. FIG. 24 shows the opposite side of the nozzle plate 1110. The nozzle plate comprises a plurality of nozzles 1010, which are set in the nozzle array 1112 (see Nozzle Bank 1011) described above. In an alternative embodiment, the nozzle array 1112 may be configured to be removable. The ability to remove the nozzle array allows it to be adapted even if the nozzles are corroded or if the nozzle dimensions need to be changed (eg when using different fluids with different viscosities). become.

FIG. 25 shows the outlet side of the fluid in the nozzle plate from which the nozzle bank has been removed. FIG. 26 shows the inlet side of the fluid in the nozzle plate of FIG. 25. 25-26 show that row 1113 of the nozzle is removable from the nozzle array assembly 1120 and the nozzle bank 1113 is removed. The ability to remove the nozzle bank 1113 allows the user to clean the nozzle plate 1120 or replace only the damaged nozzle bank 1113 instead of replacing the entire plate. In addition, the removable nozzle bank 1113 helps adjust the specific area of the contactor and aids the manufacturing process (eg, gas phase molecules with very high mass transfer can capture or react yield). Does not require much specific surface area to meet). Therefore, nozzle banks can potentially be removed for the purpose of reducing the flow rate of all liquids in existing systems.

For example, in one embodiment, the nozzle bank or nozzle row 1113 shown in FIGS. 25 and 26 was cut from a flat tube 1130 (see FIGS. 27 and 28). Tube 1130 was cut lengthwise from a suitable tube and formed from a slightly flattened or flat sheet on top of the mandrel. Multiple nozzles 1010 were cut into tubes 1130. This is an alternative method of nozzle bank formation. Tube 1130 is shown flat and is provided with a groove formed by an electric discharge machine (EDM) for orifice manufacturing. Cutting the tube 1130 in the longitudinal direction and removing the uneven ends effectively completes the groove 1113 and is ready to fit into the nozzle plate 1120.

&lt;Gas-liquid contactor&gt;

FIG. 29 is a schematic cut-out view of a gas-liquid contactor according to another embodiment of the present invention. The gas-liquid contactor can increase the efficiency of the COIL gas-liquid contactor and reduce air entrainment, as described herein. The nozzle of the gas-liquid contactor is configured to form a stable, planar liquid jet that can maintain its shape in the air stream.

These nozzles can be manufactured in an array of nozzle plates that form a densely packed, parallel matrix of planar liquid jets. The flat jet array has an aerodynamic shape and can provide stable jet formation in relatively high airflow. That is, the nozzle array is configured to form a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbances from the gas. In addition, the nozzle array produces a liquid sheet parallel to the airflow, providing a relatively large contact area and a low pressure drop. The airflow may be across the liquid jet (crossflow), backflow, or parallel.

The liquid pressure drop required to generate the jet at the nozzle is also low, which results in low pump costs on both the liquid and gas sides. A hydraulic drop occurs over an orifice (eg, a nozzle array) that imposes a major constraint. For example, the hydraulic pressure range in which this embodiment works is between 2 psi and 50 psi, and the best range is between 3 psi and 15 psi. In addition, liquid pressures of less than 2 psi can still form thin flat jets (depending on the size of the nozzle), but the speed of the liquid will be slower and significant deflection will occur in high speed airflow. Similarly, pressures above 50 psi can produce good thin flat jets, but the energy required to provide this water pressure is high, increasing the parasitic energy loss of the system.

In addition to these advantages, the nozzle does not atomize the liquid, which significantly reduces liquid entrapment in the gas compared to systems that atomize the liquid. Gas-liquid contactors have a very large specific area (eg 20 cm)^-1), This results in high contact efficiency and a small footprint (eg 100ft for contactors and support pumps).²(Less than / MV) is realized. Table 2 shows the specific area of the gas-liquid contactor and other parameters.

With reference to FIG. 29, gas-liquid contactors are generally indicated by reference number 1600. In this embodiment, a cross current configuration is used in which the gas flows from left to right in the contactor 1600. The liquid enters the upper 1610 of the contactor 1600 from the inlet plenum 1630 and flows strongly through the nozzle plate 1640 above the contact chamber 1650. The flat liquid jet is formed by these nozzles and flows down the chamber. The gas flows between parallel jets from left to right in the system of Figure 29, where mass transfer occurs and then through the low pressure descent demister 1660 towards exit 1670. The liquid is collected through the anti-splash grid 1680 on the bottom of the contactor, treated appropriately and possibly recycled. The anti-splash grid submodule 1680 is a grid with holes shaped to receive flat jets. Anti-splash guards or gas / fluid separators are also configured to substantially minimize backsplash of operating liquids. The holes in the anti-splash grid 1680 are arranged at a slight angle to the outlets 1700 and / or 1690 of the liquid capture outlet Plenum 1620 to allow the fluid to flow out without pressurizing the fluid.

Tables 2 and 3 below compare the contact efficiency and advantages / disadvantages of several gas-liquid contactors (including those of the present invention).<tables num="2"><img id="000004" he="95" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables><tables num="3"><img id="000005" he="188" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

Gas-liquid contactors were originally used in COIL's chemical reactors, but are not limited to this application. Gas-liquid contactors can be used in a number of different applications, such as high efficiency, single stage, low cost, and any application where a small footprint contact between gas and liquid is preferred. To give a few examples, heat transfer such as cooling of gas where gas and liquid come into direct contact, mass transfer such as absorption of pollutants from flue gas stream, chemical reaction between liquid and gas such as COIL application, and Biological reactions such as aerobic digestion can be mentioned. Multi-stage cross-flow contact is performed by connecting contactors in series and pumping the liquid from the outlet of the downstream contactor to the inlet of the next upstream contactor. Alternatively, two different liquid sorbents or reactants can be independently pumped into a DC-equipped gas-liquid contactor to cause a two-step reaction without disturbance of a single train stream. Embodiments of gas-liquid contacts have characteristics such as very high volume mass transfer coefficient, low pressure drop, low hydraulic drop, relatively small size, resistance to clogging, low liquid contamination, low capital and operating costs. Create a gas-liquid contactor. It is an orifice plate with a special array of nozzles that forms a matrix of flat, stable, non-fog liquid jets that are densely packed parallel to each other and parallel to the airflow (nozzles herein). It is done using a board). An embodiment of a single-stage gas-liquid contactor will be described below. The gas flow rate and multiple jet rows determine the contact time for this single step.

In this embodiment, the jet plate is housed in a gas-liquid contactor 1600. Gas enters from 1672 on the left, passes through a flat liquid jet in contact chamber 1650, passes through demister 1660, and exits at gas outlet 1670. Liquid enters from the input plenum 1630 and flows down a series of nozzle plates 1640 with great force to form a flat liquid jet, then through the gas-liquid separator 1680 and into the liquid collection chamber 1620 at the bottom of the contactor. The liquid then exits outlets 1690 and 1700 for processing and / or recycling.

FIG. 30 shows a schematic arrangement of a plurality of gas-liquid contactors in another embodiment of the present invention. With reference to FIG. 30, the multi-stage cross-flow device contactors are generally represented by reference number 3000 and are connected in series. The multi-stage cross-flow device contactor 3000 includes a first gas-liquid contactor 3002, a second gas-liquid contactor 3004, and a third gas-liquid contactor 3006. Of course, there may be more than 3 gas-liquid contactors (eg, the number of gas-liquid contactors can be determined depending on the application). That is, the number of contactors utilized is determined as a function of the final capture or reaction yield required by a particular chemical. The continuous contactor may be a concept substantially similar to the continuous chemical extraction known in the art. The airflow passes through each contactor and the liquid flows as a cross current from the downstream end 3008 to the upstream end 3010 of the train.

A liquid pump (not shown) between each stage provides liquid to each contactor. As an option, a single liquid supply plenum can provide functionality for gas-liquid contactor modules all installed in series, for which a single liquid pump can supply that liquid to a single unit. It only needs to be delivered to the series liquid supply plenum or in parallel from a single pump plenum.

The gas-liquid contactor can be formed from a variety of different materials. For example, the contactor can be made of stainless steel. Materials may be selected based on liquid and / or gaseous chemicals and their corrosiveness or reactivity (eg copper, nickel, chromium, aluminum, and alloys thereof). In addition, coated components or pipe materials can be utilized (eg, glass-lined, epoxy resin or particle coated, etc.). Alternatively, some of the structural and / or fluid treatment components of the contactor may be made of plastic or polymer, fiber reinforced epoxy resin or polymer, structural polymer, polyimide, and mixtures and compounds thereof.

&lt;Removal of pollutants with ammonia water&gt;

The embodiments of the present invention described herein can be used to remove pollutants from exhaust gas by utilizing ammonia. An important cost driving factor for pollutant removal is low partial pressure of pollutants in combustion exhaust gas or low gas absorption rate. For example, the reaction rate is generally determined as a function of the initial concentration of the reactants, the higher the concentration, the faster the reaction. However, low initial concentrations make mass transfer a variable that imposes constraints on the reaction or removal of gas or liquid molecules. In embodiments of the invention, the low mass transfer coefficients are offset by a high relative area and a high flow rate.

In related technology, we have developed a combustion exhaust gas (FGD) desulfurization system and installed it in a power plant to SO.₂And SO₃Is tackling the problem of acid rain and air pollution. Most FGD systems are SO by bringing the flue gas into contact with moist limestone.₂CaSO₃Absorb as, then CaSO₄Oxidize to (gypsum), precipitate, sell or landfill. Disadvantages of lime or limestone based FD are various pollutants (eg NO_x, Hg, or CO₂) Cannot be supported. Another drawback is that the FGD system requires a large footprint and capital investment (eg spray towers and oxidation tanks, etc.).

Suitable for high gas absorption and removal, sorbents have characteristics such as high liquid jet performance, high gas loading capacity, high oxidative stability, low heat of reaction, low sorbent cost, low corrosiveness, and commercially available product stream. It is a system to have. An example of Sovent is ammonia water. NO by selective catalytic reduction (SCR) or selective non-catalytic reduction (SNCR) by injecting ammonia, ammonia salts, and uric acid into the boiler or flue gas._xCan be reduced. Ammonia and its salts are SO_xAnd can control multiple pollutants.

In addition, in the control of multiple pollutants using aqueous absorbers by related technology, NO of combustion exhaust gas_xNO, which is the main component of, is N by selective catalytic reduction (SCR) or selective non-catalytic reduction (SNCR).₂Reduced to, or NO₂NO needs to be oxidized to water because it has a very low solubility in water. NO₂NO if oxidized to_xCan be absorbed with a basic solution or nitric acid. Valuable by-products are produced when utilizing ammonia-based systems. Ammonium nitrate and ammonium sulfate can be used as fertilizers. Ammonia is more CO than monoethanolamine (MEA) or diethanolamine (DEA)₂Efficient to capture and CO₂Is an excellent means of recovering oil fields.

Embodiments of the present invention include several target pollutants (eg, acid gas, ammonia, VOCs, SO)._x, NO_x, CO₂, Hg, and combinations thereof, but not limited to these) can be captured. In addition, some embodiments of the invention have a single, small footprint, system and are configured to produce valuable by-products. In addition, in the embodiment there is no contact with the slurry, which does not make it difficult to process the associated material. Ammonia regenerator (or CO) by not using slurry₂It is no longer necessary to utilize the heat that completes the phase change in the stripper).

In an embodiment of the invention, the flue gas is removed by cleaning the fly ash with a bag house or electrostatic precipitator (ESP) and, as appropriate, cooled for a first wet contact. And SO of combustion exhaust gas₂And NO may be oxidized with gaseous hydrogen peroxide, or oxidized with a first gas cleaning device using an aqueous hydrogen peroxide solution. The gas cleaning device is a horizontal cross-flow gas-liquid contactor with high efficiency and a small footprint, as described herein. The gas cleaning device cleans the fuel exhaust gas with basic aqueous ammonium sulfate and acid gas (SO).₂, SO₃, NO₂, HCl, HF, etc.). Make-up ammonia is added for pH control to supply hydroxide ions to react with the hydrogen ions produced by the hydrolyzed gas. This converts the gas into a soluble ammonium salt and its vapor pressure drops to almost zero. SO_xBetter results than about 99% absorption of. Mercury can also be removed by oxidation and / or absorption processes (HgO)_xIs much more soluble than the element Hg). Some reaction mechanisms for pollutant removal in some embodiments of the present invention are as follows. NH₃Hydrolysis: NH₃ + H₂O NH₄⁺ + OH^- (1) SO₂capture: H₂O + SO₂ H⁺ + HSO₃^- (2) 1 / 2O₂ + HSO₃^- HSO₄^- (3) 2NH₃ + HSO₄^- + H₂O (NH₄)₂SO₄ + OH^- (Ammonium sulfate) (4) NO_xcapture: NH₃ + H₂O NH₄⁺ + OH- (5) H₂O₂ + OH^- HO₂^- + H₂O (6) HO₂^- + NO NO₂ + OH^- (7) 2NO₂ + H₂O₂ 2HNO₃ (8) NH₃ + HNO₃ NH₄NO₃ (Ammonium nitrate) (9) Hg capture H₂O₂ + Hg⁰ Hg (II) + product (10) H₂S capture H₂S (aq) HS^- + H + (11) HS^- + NH₃ + H⁺ NH₄HS (12)

Sulfur and nitrogen oxides are salts (NH₄) NO₃And (NH₄)₂SO₄Once captured as, the contact solution concentrates and precipitates and is sold or processed. Heavy metals (Hg) and halides (Cl and F) are separately precipitated at the pH adjustment step. The diluted contact solution is recycled into a gas washer.

Combustion emissions through these processes are even better than clean, with 95% of all pollutants removed, and partially CO.₂Ready to remove. The second gas cleaning device utilizes a combination of aqueous ammonia and / or an ammonia salt as a liquid. CO₂Is absorbed and reacts with ammonium carbonate and water to form ammonium bicarbonate. CO for low and high pH₂Absorption is preferred. Supplemental ammonia controls the pH and the level of free ammonia in the gas wash solution. When the concentration of ammonia is high, the pH rises and CO₂Absorption and CO₂The load of ammonia increases, and the vapor pressure of ammonia rises. The embodiment of the present invention the CO definitive₂Simplified reaction mechanisms for capture include: 2NH₃ + H₂O + CO₂ (NH₄)₂-CO₃ (Ammonium carbonate) (13) (NH₄)₂ CO₃ + CO₂ + H₂O 2NH₄HCO₃ (Ammonium bicarbonate) (14)

CO the concentrated solution from the contactor₂It is sent to a stripper, where it is heated, a reverse reaction takes place, and gaseous CO₂Is released and ammonium carbonate is produced. CO for high and low pH₂Is preferred. Ammonia absorption is suitable for low pH, so low pH causes CO₂Release is promoted and ammonia can be retained in solution. CO₂Is separated and compressed to return the ammonium carbonate to the gas washer.

A common problem with ammonia-based systems of related technology is the "ammonia slip" in which the ammonia dissolved in the absorbing liquid returns to the gas phase and the stack in the flue gas accumulates. This phenomenon results in a visible plume when ammonia reacts with the constituents of the flue gas to precipitate a solid. In addition, ammonia slip significantly increases reagent costs.

In one embodiment, a plurality of gas-liquid contactors shown in FIG. 30 are used for pollutant removal. In this embodiment, each gas and liquid can be configured for different purposes. For example, the gas-liquid contactor 3006 may be specifically designed to capture all of the ammonia that could slip on each of the first two contactors 3002 and 3004. In this embodiment, acid gas (SO)_x, NO_x, And CO₂The optimum pH for absorbing) is above 7, because the vapor pressure of these gases is lowest at high pH, but the vapor pressure of ammonia is highest at high pH. SO better than about 99% under the optimum conditions of the first gas-liquid contactor 3002₂Can be captured. The third contactor 3006 can operate the first gas-liquid contactor 3002 and the second gas-liquid contactor 3004 under optimal conditions for absorbing acid gas with high ammonia slip. Yes, because the third contactor 3006 operates under optimal conditions for capturing ammonia. The captured ammonia is returned to the first two gas-liquid contactors. The high efficiency and small size of the gas-liquid contactor means that a third gas-liquid contactor can be provided, which means that a very high capture efficiency is achieved.

In this embodiment, a plurality of types of efficiencies (achieve high efficiency of removing a plurality of pollutants from the flue gas by reducing the cost of the energy consumption and removal system, and minimize the size of the removal system from the flue gas. Achieves high efficiency in removing multiple pollutants, and removes multiple pollutants from flue gas by creating a modular system that can be combined in parallel to accommodate different equipment sizes. From combustion emissions by creating a modular system with very low flow resistance (pressure drop) that can be combined in series to enable high efficiency, selective and continuous removal of contaminants. Modular system combined to provide high efficiency achievement, duplication (high availability) and maintainability (selective access for periodic maintenance or in case of unit failure) to remove multiple pollutants Achieve high efficiency in removing multiple pollutants from flue gas by creating, and remove multiple pollutants from flue gas by creating a modular system that can be mass-produced in the assembly line process Achievement of high efficiency and high efficiency of removing multiple pollutants from flue gas from various types and sizes of power generation and chemical process equipment) have been achieved.

Further embodiments are described as methods and systems in which the selectively high mass transfer of pollutants in the flue gas from a large volume flue gas flow rate is made into a continuously replenished liquid constrained by a small system volume. sell. In the method and system, a high-viscosity, wide-ranging, thin, long, stable jet high-density filling array reacts with a high-speed flue gas flow. The orifice forming the jet can be optimized based on the properties of the liquid saw vent, such as viscosity and surface tension. The cross-flow and back-flow designs represent two different embodiments.

The efficiency of the method and system is the large mass transfer of volume and the resulting compactness, low pressure combustion treatment requiring minimal pumping function, and the low resistance and design modularity of the aerodynamically formed jets. And it is achieved by the pressure drop of the low pressure combustion exhaust gas of the whole system due to the low resistance due to the combinational nature. See also Table 3-4. This dramatically increases the efficiency of the process of removing pollutants from combustion emissions, and CO₂, SO_x, NO_x, And the removal of pollutants such as Hg is economically possible.

In another embodiment, the smaller scale version can be easily adapted to the exhaust of large commercial means of decontamination. In yet another embodiment, volatile organic compounds from the chemical plant are removed from the exhaust. In yet another embodiment, a very dry airflow can be achieved by utilizing a cold liquid stream. In another embodiment, the particulate matter can be removed by increasing or decreasing the humidity of the gas.

FIG. 31 is a schematic diagram of a plurality of pollutant removal systems in one embodiment. In Figure 31, multiple pollutant removal systems are generally indicated by reference number 2100. System 2100 is SO_x, NO_x, CO₂, Hg, HCl, and HF may be captured. In the present embodiment, the combustion exhaust gas 2120 from the boiler 2110 is first washed at a specific removal point 2130 (for example, a settling chamber or a net filter) to remove fine particles such as fly ash, and is appropriately cooled at the cooling station 2140. .. At 2150, the fuel gas is about N₂, H₂O, CO₂, SO₂, NO, Hg, HCl, and HF. This, of course, depends on the processing of the boiler 2110. The flue gas is then contacted with aqueous ammonia and dissolved ammonia salts in a highly efficient gas-liquid contactor 2160 as described herein. The dissolved ammonia salt is from recycle stream 2170, from suspended matter 2110 from precipitation step 2190, ammonium sulphate (SO).₃), Sulfate (SO₄), Nitrate (NO₃), Chloride (Cl), Fluoride (F), and possibly small amounts of carbonate (CO)₃), And bicarbonate (HCO)₃)including. Ammonium carbonate and ammonium bicarbonate may be kept to a minimum by utilizing approximately stoichiometric amounts of supplemental ammonia.

In step 2165, the liquid phase is oxidized with the gas-liquid contactor described in the embodiment of the present invention. Of course, NO is NO using some oxidizers.₂Can be converted to and better absorbency can be obtained. SO₃^-Also liquid phase SO₄^2-Oxidize. A liquid bleed stream 2220 is sent to the precipitator to remove heavy metals and ammonia salts. In the first step 2230, heavy metals (Hg, etc.) are precipitated by pH adjustment 2210. In the second step 2190, the liquid is concentrated to precipitate the ammonia salt. The heavy metal solids from the precipitation step are properly treated (2240) and the ammonium salt solids are sold as fertilizers (2250). If the ammonia salt can be sold as a concentrated liquid fertilizer after Hg removal, the second precipitation step can be omitted.

Then N₂, H₂O, and CO₂The fuel exhaust gas 2120 containing only is contacted with ammonia and dissolved ammonium carbonate / ammonium bicarbonate in another high efficiency gas-liquid contactor 2260 described herein. Again, the ammonia is the replenishment stream and the dissolved salts are from the recycle stream 2270. Ammonia is added to the object to keep the pH of the contact liquid optimal. CO₂Is CO₂It is absorbed as ammonium bicarbonate in the liquid sent to the stripper 2280. Here, the temperature is raised (and the pH is adjusted if necessary), the reverse reaction is carried out, and CO₂Is released as gas 2290, leaving ammonium carbonate in liquid phase 2300, CO₂Recycle to absorber. CO₂Is then compressed (2310) and may be sold or quarantined (2320). Degraded natural gas wells, secondary oil recovery, and other methods can be used for quarantine treatment, but these are outside the scope of the present invention and will not be described in detail.

CO₂After the absorption step, the flue gas is brought into contact with water in a third high efficiency contactor 2330 as described to strip out any ammonia that could slip from the previous contactor. The pH of the contact liquid (water) is adjusted as necessary to completely absorb ammonia. Bleedstream 2340 CO₂Stripper 2300 or SO_xMay be sent to the absorber.

Finally, nitrogen, water, some oxygen, and unabsorbed CO₂The washed flue gas 2350 composed of is heated by 2360 to reduce the condensation state and sent to the ID fan 2370 and the stack. By interconnecting the combustion exhaust gas heater 2360 and the cooler 2140 to a liquid heat carrier, the process can be carried out economically. The cooling liquid is brought into contact with the hot combustion exhaust gas in the gas-liquid heat exchanger 2140. The cooled combustion exhaust gas is sent to the first absorber 2160. Now the hot liquid is sent downstream to the flue gas heater 2360 and brought into contact with the cooled flue gas 2350 from the final absorber 2330. The gas-liquid heat exchanger 2360 cools the liquid sent back to the cooler 2140, heats the combustion exhaust gas 2350, and prepares the exhaust gas to the surroundings. Hot liquids are also CO₂It can also be used as a heat input to the stripper 2300.

As an option, CO is used for exhaust heat generated in industrial processing.₂Dew-proof treatment can be omitted by using it as a heat source for reheating the strip or exhaust gas. For example, in a power plant this can be obtained from a fly ash bag house.

Also, as an option, CO as appropriate₂The process can also be modified to omit the capture process. That is, SO the system_x, NO_x, Hg, HCl and HF capture treatment, and the production of ammonium sulphate and nitrate as fertilizers can be emphasized.

FIG. 32 is a schematic diagram of a multiple pollutant removal system according to another embodiment of the present invention. The processing in Figure 32 is SO_x, HCl, and HF only have been simplified to capture only. Treatment 2400 is designed to capture only the most easily absorbed acid gases. The combustion exhaust gas 2120 from the boiler 2110 is first washed at a specific removal point 2130 (eg, settling chamber or net filter) to remove fine particles such as fly ash, and is appropriately cooled at the cooling station 2140. At the time of 2150, the combustion exhaust gas is almost N₂, H₂O, CO₂, SO₂, NO, Hg, HCl, and HF.

The flue gas 2150 is then contacted with sodium hydroxide or sulfate / sulfite salt from the recycle stream 2420 within the high efficiency gas-liquid contactor 2410, as described herein. Oxidation step 2430 is performed in the liquid phase in a gas-liquid contactor. Sulfites (SO) using oxygen contained in the air or combustion exhaust gas₃^2-) By oxidizing the liquid phase sulfate (SO)₄^2-) Occurs. A liquid bleed stream 2440 is sent to the precipitator 2450 to remove heavy metals and sulfates. In the first step 2460, heavy metals (Hg, etc.) are precipitated by pH adjustment 2460. In the second step, calcium hydroxide 2470 can be added to precipitate calcium sulphate, which can be separated, dried and removed with a precipitator 2480. The suspended matter 2490 from this settler is returned to the recycling stream. Heavy metal solids produced during the precipitation step may be treated appropriately (2510) and calcium sulphate can be sold as gypsum (2520).

Finally, nitrogen, water, NO_x, And CO₂The washed flue gas 2350 composed of is heated by the heater 2360 to reduce the condensed state and sent to the ID fan and the stack 2370. As mentioned above, the process can be carried out economically by interconnecting the flue gas heater 2360 and the cooler 2140 with a liquid heat carrier.

&lt;SO₂Removal&gt;

SO₂Various performance areas for improving capture capabilities include reducing the vessel size and pressure drop of the reactor and utilizing efficient mass transfer sorbent systems that produce commercially available by-products. .. High SO to achieve these targeted performances₂There is a need for innovative design methods that combine absorption dynamics with value-added production streams.

The gas-liquid mass transfer process is performed along the gas-liquid interface. The absorption rate of gas into a liquid soap is the liquid phase mass transfer coefficient k._L, Specific surface area (ratio of surface area of gas-liquid interface to volume) a, and bulk fluid C_LAnd gas-liquid interface C_L^*It is controlled by the concentration gradient between and. In many gas-liquid reaction systems, C_L^*Is low in solubility and there is a limit to the control of the concentration gradient. In order to increase the gas absorption rate, in the embodiment of the gas-liquid contactor, mass transfer dynamics, gas-liquid mixing and / or a method of increasing the ratio of the interface surface area to the volume is adopted.

In the embodiment of the present invention, SO₂Cooler Imstone / Lime (CaCO)₃), Sodium carbonate (Na₂CO₃) / Sodium hydroxide (NaOH), ammonium hydroxide (usually called aqueous ammonia, abbreviation AA), double alkali (sodium hydroxide with lime added), magnesium oxide (MgO), oxidation The contactor can be utilized with a wide variety of aqueous solvents including, but not limited to, zinc (ZnO). SO by adding oxidizer (OX)₂Oxidation is promoted, which promotes sulfate SO₄^2-Formation is promoted. In a preferred embodiment, the OX agent is hydrogen peroxide (H).₂O₂). The combined use of aqueous ammonia and hydrogen peroxide is particularly preferred as it produces a profitable by-product stream such as ammonium sulphate (fertilizer). In addition, H₂O₂Decomposition products (water and oxygen) are environmentally and equipment friendly.

SO when aqueous ammonium hydroxide and hydrogen peroxide are included₂The chemical steps available for oxidation are: NH₃ + H₂O + SO₂ NH₄⁺ + HSO₃^- (1) NH₄⁺ + HSO₃^- + NH₃ 2NH₄²⁺ + SO₃^2- (2) H₂O₂ + SO₃^2- H₂O + SO₄^2- (3) 2NH₄⁺ + SO₄^2- NH₄SO₄ (Ammonium sulfate) (4)

In the embodiment of the present invention, sulfur dioxide is removed with high efficiency by the exhaust gas cleaning treatment. The system of this embodiment includes a nozzle array with a reformed orifice plate (or the nozzle plate described) and a fluid synthesis technique suitable for a wide range of fluids and processing conditions. SO₂Is removed by passing the gas from a high surface through the volumetric gas-liquid contact unit. Exhaust gas passes horizontally through a gas-liquid contactor, which has a substantially smaller contactor volume and airflow pressure drop than related technologies (referred to as crossflow). Multiple low pressure, vertical flat jet arrays with aqueous sorbents and substantial surface area run across cross currents. The aerodynamic shape of the flat jet array forms a stable jet flow with less mixing of liquid particles at relatively high gas velocities.

In a preferred embodiment, the sorbent for the absorption and removal of sulfur dioxide has a high SO.₂The system has properties such as capacity, high oxidative stability, low heat of reaction, low sorbent cost, low corrosiveness, and a commercially available product stream. Effective SO₂An example of a solvent for removal is an aqueous solution containing 28% by weight of ammonia. In order to optimize the contactor, from the viewpoint of fluid and jet performance, about 1% to about 2% polymer or suspension can be added to the aqueous ammonia solution to enhance the contactor performance. Examples of additives include those that do not react with aqueous ammonia and do not interfere with mass transfer. The polymer or suspension allows the formation of sorbent properties (eg, viscosity) that allow for maximum jet performance (jet width, length, thickness, surface area) with minimal liquid side pressure drop. Examples of polymer additives include diethylene glycol. Examples of other polymer additives include polyethylene oxide or polyvinyl alcohol. An example of an inorganic additive is bentonite.

Including additional chemical compounds is SO₂Oxidation rate and thus suitable for assisting mass transfer dynamics. Hydrogen peroxide is an example of an additive to a suitable sorbent system. Stabilizers are added to the sorbent mixture to prevent hydrogen peroxide from decomposing too much at high pH. An example of a hydrogen peroxide stabilizer at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide can be further improved by adding a catalyst of hydrogen peroxide. An example of a hydrogen peroxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

FIG. 33 is a schematic diagram of a typical gas-liquid contactor that causes an interaction between a gas phase and a liquid phase in another embodiment of the present invention. The gas-liquid contact system includes a gas inlet 2600 that is connected to a gas supply unit 2605 to supply gas to the gas-liquid contactor 2645. The system further includes a liquid reagent tank 2610 connected to a pump 2615 and a liquid capture tank 2620. The capture tank 2620 collects liquid from the gas-liquid contactor 2645 by being connected to the gas-liquid contactor 2645. Optionally, the capture tank 2625 may be connected to a liquid recirculation pump 2625. The liquid recirculation pump 2625 can perform the liquid recirculation method. The flow control valve 2630 controls the liquid to the liquid plenum 2635 by being connected to the liquid plenum 2635. A nozzle array 2640 for forming the liquid jet is connected to the liquid plenum and the gas-liquid contactor 2645. The gas-liquid contactor 264 includes a gas-liquid jet contact zone. A gas-liquid separator 2650 that separates the gas from the liquid soap vent jet is placed inside the gas-liquid contactor 2645. A demister 2660 capable of removing small gas droplets from the outgoing gas is placed near the gas outlet 2655.

The gas inlet may contain a plurality of different gases. For example, SO_x, NO_x, CO₂, Hg, and industrial emissions of pollutants, contaminants, etc. that may contain combinations thereof. Of course, HCl, HBr, HF, H₂SO₄, HNO₃, CO, H₂Removes S, amines (including ammonia), alkanolamines, ureas, formamides, alcohols, carboxylates (acetic acid, etc.), combinations thereof and other gaseous molecules such as acid gases such as a wide variety of other gas phase molecules. You can also do it. The limitation of the present invention is only the function of providing a gas phase molecular reactant or solute, and a liquid phase in a range that is reactive or soluble. Although the main description of the specification of the present invention is intended for aqueous solutions, it is easy to understand that the invention of a serious liquid contactor can be applied to a non-aqueous system.

In this embodiment, SO₂A method of injecting an exhaust gas containing the above into a gas-liquid chamber is described. The gas plenum allows the gas to flow evenly throughout the liquid flat jet. The liquid jet is generated by pumping the saw vent into the liquid plenum and spreading the saw vent across the nozzle orifice. The resulting jet flows vertically downward into the contact chamber and reaches the capture tank through the gas-liquid separator. In a gas-liquid chamber, a vertically flowing sorbent intersects a crossflow of gas. Sulfur dioxide is absorbed by the sorbent liquid and removed from the exhaust stream. The exhaust gas after cleaning is discharged from the outlet of the contact chamber. Sovent is recirculated and continuously SO from the exhaust stream₂To remove.

The performance of the gas-liquid contactor is shown on the small subscale testbed in Figure 33. Table 4 summarizes the geometric parameters in this example.<tables num="4"><img id="000006" he="47" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

The configuration of the jet orifice used in this example is described in the context of the nozzle plate and gas-liquid contactor. Prior to processing, the surface area of the liquid jet is optimized for jet length, width, and thickness by varying the pump support pressure on the jet orifice plate. Further optimizations regarding jet surface area (length and width) are possible by utilizing additives (eg, diethylene glycol) to improve sorbent viscosity / surface tension properties or by reforming the orifice nozzles.

Table 5 shows an example of the operating conditions and performance of the gas-liquid contactor. A sorbent system containing approximately 28% by weight aqueous ammonia was tested. No additives involved in viscosity or oxidation were added to the Sovent mixture. As exhaust gas, N₂SO₂Was added by 500ppmv. A mixture of gases was injected into the contactor under atmospheric temperature and atmospheric pressure conditions and measured using a carved mass flow controller. The volumetric flow rate of the liquid was measured by recording the amount of liquid jet discharged into the carved recipient container at the measured time intervals. SO under the above test conditions₂Test results on absorption show oxidant accelerator (H)₂O₂95% SO without using)₂Was removed.<tables num="5"><img id="000007" he="58" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;NO_xCapture device&gt;

Another embodiment of the present invention is NO by utilizing a gas-liquid contactor._xRegarding the capture of. NO_xAre mainly nitric oxide (NO) and nitrogen dioxide (NO)₂) Is the main pollutant. NO, depending on the combustion process_xNitrogen oxides account for more than 90% of the total. NO_xIs caused by the reaction of nitrogen and oxygen at high combustion temperatures (&gt; 2700 degrees Fahrenheit) and by the oxidation of nitrogen in the fuel. NO₂Various performance areas for improving the capture function include reducing the vessel size and pressure drop of the reactor and utilizing an efficient mass transfer sorbent system.

The gas-liquid mass transfer treatment is performed at the gas-liquid interface. The absorption rate of gas into a liquid soap is the liquid phase mass transfer coefficient k._L, Specific surface area (ratio of surface area of gas-liquid interface to volume) a, and bulk fluid C_LAnd gas-liquid interface C_L^*It is controlled by the concentration gradient between and. In many gas-liquid reaction systems, C_L^*Is low in solubility and there is a limit to the control of the concentration gradient. In order to increase the gas absorption rate, the gas-liquid contactor needs to be designed to increase the ratio of mass transfer dynamics, gas-liquid mixing and interfacial surface area to volume.

One embodiment of the present invention includes a high performance gas-liquid contactor as described, for example, with reference to FIG. 33. The system can improve overall mass transfer and contactor performance by utilizing a thin flat jet with high density, large surface area and aerodynamic shape. Gas-liquid contactor is about 1 cm^-2About 50 cm from^-2The improved specific surface area, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop of the contactor is as low as less than 5 torr / linear ft, and the liquid jet drive pressure is low. It is characterized by less than 50 psi (more preferably less than 20 psi) and minimal mixing of liquids into the gas stream.

In a preferred embodiment, the system is about 10 cm.^-1About 20 cm from^-1The specific surface area in the range of, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop of the contactor is as low as less than 1 Torr / linear foot, and the jet drive pressure is about 5-10 psi. It is characterized by being in the range and minimizing the entry of liquid into the gas stream.

NO_xGas-liquid contact with a wide variety of aqueous sorbents containing, but not limited to, ammonium hydroxide (usually referred to as aqueous ammonia, abbreviated as AA), metal chelate or uric acid for efficient capture. You can use the vessel. NO NO by adding oxidizer (OX)₂Oxidation to is promoted, which increases the solvent absorption rate. Sodium chlorite (NaClO) for various oxidants (OX)₂), Sodium hypochlorite (NaOCl) Sodium hydroxide-potassium permanganate (KOH-KMnO)₄), And hydrogen peroxide (H)₂O₂) Is included. In a preferred embodiment, the contactor utilizes aqueous ammonia and hydrogen peroxide, because H₂O₂Degradation products (water and oxygen) are environmentally and equipment friendly, both of which do not spoil the normal materials of the structure and can be sold as fertilizers for crops, leading to reduced processing costs. Produces ammonium sulphate that can be produced.

NO and NO when ammonium hydroxide and hydrogen peroxide are included₂The oxidative chemistry mechanism of is thought to be as follows. NH₃ + H₂O NH₄⁺ + OH^- (1) H₂O₂ + OH^- HO₂^- + H₂O^- (2) HO₂ + NO NO₂ + OH^- (3) NO₂ + NO₂ N₂O₄ (Four) N₂O₄ + H₂O HNO₂ + HNO₃ (Five) HNO₂ + H₂O₂ HNO₃ + H₂O (6) HNO₃(Aqueous) H⁺ + NO₃^- (7) NH₄⁺ + NO₃^- NH₄NO₃ (Ammonium nitrate) (8)

In one embodiment, an exhaust gas cleaning treatment that removes sulfur dioxide with high efficiency is utilized. The system includes a nozzle array. The nozzle array has a reformed orifice plate (or nozzle plate) and includes a wide range of fluids and fluid synthesis techniques to suit processing conditions. In this embodiment, NO_xIs removed by passing the gas from a high surface through the volumetric gas-liquid contactor unit. Exhaust gas passes horizontally through a gas-liquid contactor with a substantially smaller contactor volume and airflow pressure drop (referred to as crossflow). Multiple low pressure, vertical flat jet arrays with aqueous sorbents and substantial surface area run across cross currents. The nozzle array is aerodynamically shaped to generate a flat jet array that forms a stable jet stream with less mixing of liquid particles at relatively high gas velocities.

In embodiments of the present invention, the sorbent for the absorption and removal of sulfur dioxide has a high NO._XIt may include systems with properties such as capacity, high oxidative stability, low heat of reaction, low solvent cost, low corrosiveness, and commercially available product streams. In a preferred embodiment, an effective NO₂An example of a solvent for removal is an aqueous solution containing 28% by weight of ammonia. Optimize nozzle plates (described here) by adding about 1% to about 2% polymer or suspension to aqueous ammonia to enhance contactor performance in terms of fluid and jet performance. Can be done. Suitable additives are those that do not react with aqueous ammonia and do not interfere with mass transfer. Polymers or suspensions can be utilized that allow the formation of sorbent properties (eg, viscosity) that allow maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. Examples of polymer additives include diethylene glycol. Examples of other polymer additives include polyethylene oxide or polyvinyl alcohol. An example of an inorganic additive is bentonite. The inclusion of additional chemical compounds is suitable to aid in the oxidation rate of NO and thus mass transfer kinetics. Hydrogen peroxide is an example of an additive to a suitable sorbent system. Stabilizers are added to the sorbent mixture to prevent hydrogen peroxide from decomposing too much at high pH. An example of a hydrogen peroxide stabilizer at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide is further enhanced by adding a catalyst of hydrogen peroxide. An example of a hydrogen peroxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

As explained with reference to Figure 33, NO_xIt can be used for capture. NO process to gas-liquid chamber 2645_xThis will be described by injecting exhaust gas containing. The gas plenum 2605 evenly distributes gas throughout the liquid flat jet. The liquid jet is generated by pumping the saw vent to the liquid plenum 2635 and spreading the saw vent across the nozzle orifice. The generated jet flows vertically downward into the contact chamber and reaches the capture tank 2620 through the gas-liquid separator. In the gas-liquid chamber 2645, a vertically flowing sorbent intersects the crossflow of gas. Sulfur dioxide is absorbed by the sorbent liquid and removed from the exhaust stream. The exhaust gas 2655 after cleaning is discharged from the outlet of the contact chamber. The solvent is recirculated and continuously NO from the flue gas stream_XTo remove. The performance of the gas-liquid contactor is shown on the small subscale testbed in Figure 33. Table 6 summarizes the geometric parameters in this example.<tables num="6"><img id="000008" he="48" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

The configuration of the jet orifice used in this example is as described above. Prior to processing, the surface area of the liquid jet is optimized for jet length, width, and thickness by varying the pump support pressure on the jet orifice plate. Further optimizations regarding jet surface area (length and width) are possible by utilizing additives (eg, diethylene glycol) to improve the viscosity / surface tension properties of the sorbent, or by reforming the orifice nozzle.

Table 7 shows an example of the operating conditions and performance of the gas-liquid contactor. Solvent systems containing approximately 28% by weight aqueous ammonia were tested under any of the operating conditions shown in Table 2. NO as a solvent₂We used oxidants (Ox) that promote the removal of shavings or those that do not contain additives related to viscosity. Exhaust gas is NO to nitrogen (N2)₂Was added by 500ppmv. A mixture of gases was injected into the contactor under atmospheric temperature and atmospheric pressure conditions and measured using a carved mass flow controller. The volumetric flow rate of the liquid was measured by recording the amount of liquid jet discharged into the carved recipient container at the measured time intervals. Reduced NO from contactor₂Concentration is NO₂It can be measured by measuring the light absorption at 400 nm. Background NO₂Concentration of was recorded before each run. NO₂/ N₂First generate a stable flow of (A) without a jet flow_{Off Off}) Absorbance was recorded. A jet stream (28 wt% AA) was then injected into the reactor chamber and the absorbance was recorded. Reduced NO₂The amount of (the amount absorbed) is a percentage,% NO₂Reduction = 100x (A)_off-A_on) / A_off... expressed as (1).

Figure 34 shows NO₂It is a graph which shows the relationship between the absorption degree of the removal system and the runtime. In Figure 34, a typical NO due to on and off of a liquid ammonia water jet.₂The absorption spectrum is shown. The y-axis represents absorption at 400 nm and the x-axis represents time in seconds. As can be seen from this example, the short survival of the absorption immediately after the start of the jet flow is due to the perturbation of the flow in the chamber. An average of four test runs was run for each test result. NO under the listed test conditions₂Absorption test result is NO₂Removal of -35%, pro-oxidant (H)₂O₂) Was not appropriate.

&lt;Hg capture device&gt;

Another embodiment of the present invention is NO by utilizing a gas-liquid contactor._xRegarding the capture of. The gas-liquid mass transfer process is performed along the gas-liquid interface. The absorption rate of gas into a liquid soap is the liquid phase mass transfer coefficient k._L, Specific surface area (ratio of surface area of gas-liquid interface to volume) a, and bulk fluid C_LAnd gas-liquid interface C_L^*It is controlled by the concentration gradient between and. In many gas-liquid reaction systems, the graph is C_L^*Solubility is very low and control of the concentration gradient is limited. Therefore, in order to increase the gas absorption rate, it is necessary to increase the mass transfer dynamics and increase the ratio of the interface surface area to the volume.

One embodiment of the present invention includes a high performance gas-liquid contactor as described, for example, with reference to FIG. 33. The system can improve overall mass transfer and contactor performance by utilizing a thin flat jet with high density, large surface area and aerodynamic shape. Gas-liquid contactor is about 1 cm^-2About 50 cm from^-2The improved specific surface area, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop of the entire contactor is as low as less than 5 torr / linear ft, and the liquid jet drive pressure. Is characterized by less than 50 psi (more preferably less than 20 psi) and minimal mixing of liquids into the gas stream.

In a preferred embodiment, the system is about 10 cm.^-1About 20 cm from^-1The specific surface area of the range, the volume of the generator, which is about 1/10 of the volume of the packed bed of the related technology, the pressure drop is less than 1 Torr, the jet drive pressure is about 5 psi, and to the gas flow. It includes the feature that the mixing of liquid is minimized.

The gas-liquid contactor is elemental mercury (Hg)⁰) Is available with various aqueous sorbents that oxidize to Hg (II). In the Hg (II) state, mercury becomes soluble in aqueous solution, and Hg (II) can remove elemental mercury (HgO) from the exhaust stream by catalytic activity. Oxidizing agents (OX) include sodium hypochlorite (NaOCl) and hydrogen peroxide (H)₂O₂) Is included, but is not limited to these. A suitable oxidizer for use in contactors is Hg⁰Hydrogen peroxide (H) with a catalyst (Cat) added as an additive to improve the oxidation rate₂O₂). Additives are, for example, HgCl2, TAML (iron (III) tetra-amide macrocyclic ligand), catalase or peroxidase.

The chemical mechanism of Hg oxidation when aqueous hydrogen peroxide is included is believed to be as follows. H₂O₂ + Hg⁰ Hg (II) + product (1) H₂O₂ + Cat + Hg⁰ Hg (II) + product (2)

In the present embodiment, a high-efficiency gas-liquid contactor is used for the exhaust gas cleaning treatment for removing mercury with high efficiency. The system has a reformed orifice plate (or nozzle plate) and includes a nozzle array that includes a wide range of fluids and fluid synthesis techniques that suit processing conditions. Removal of Hg is performed by passing a gas from a high surface through the volumetric gas-liquid contactor unit as described in US Pat. No. 7,379,487, which is incorporated herein by reference. Exhaust gas passes horizontally through a gas-liquid contactor with a substantially smaller contactor volume and airflow pressure drop (referred to as crossflow). Multiple low pressure, vertical flat jet arrays with aqueous sorbents and substantial surface area run across cross currents. The aerodynamic shape of the flat jet array forms a stable jet flow with less mixing of liquid particles at relatively high gas velocities.

In a preferred embodiment, the absorption and removal of mercury is carried out by a system having properties such as high Hg capacity, high oxidative stability, low heat of reaction, low solve cost, low corrosiveness, and a commercially available product stream. An example of Sovent is elemental Hg⁰It is an aqueous solution containing about 10% by weight of hydrogen peroxide and about 0.1% by weight of a catalyst in order to promote the oxidation of hydrogen peroxide to Hg (II). The nozzle plate configuration may be optimized by adding a suspension of about 1% to about 2% to the aqueous solution of hydrogen peroxide to enhance the performance of the contactor. Additives may be designed so that they do not react with the aqueous hydrogen peroxide solution and do not interfere with mass transfer. Additives allow the formation of sorbent properties (eg, viscosity) that allow maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. An example of an additive is bentonite.

The inclusion of additional chemical compounds is suitable to aid in the oxidation rate of Hg and thus mass transfer kinetics. An example of an additive to a suitable solvent system is hydrogen peroxide. Stabilizers are added to the mixture of solvents to avoid over-decomposing hydrogen peroxide at high pH. An example of a hydrogen peroxide stabilizer at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide can be further improved by adding a catalyst of hydrogen peroxide. An example of a hydrogen peroxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

As described with reference to FIG. 33, this system can be utilized for Hg capture. The process is described by injecting an exhaust gas containing Hg into the gas-liquid chamber 2645. The gas plenum allows the gas to flow evenly throughout the liquid flat jet. The liquid jet is generated by pumping the soap vent to the liquid plenum 2635 to spread the solvent throughout the nozzle orifice. The generated jet flows vertically downward into the contact chamber and reaches the capture tank 2620 through the gas-liquid separator. Mercury is absorbed by the sorbent liquid and removed from the exhaust stream. In the gas-liquid chamber 2645, the vertically flowing solvent intersects the crossflow of the gas. The exhaust gas 2655 after cleaning is discharged from the outlet of the contact chamber. The sorbent is recirculated to continuously remove Hg from the exhaust stream.

&lt;H₂S capture device&gt;

Another embodiment of the present invention is H by utilizing a gas-liquid contactor.₂Regarding the capture of S. Hydrogen sulfide is a highly toxic, flammable, unpleasant-smelling gas that is considered to be toxic in a wide range, but especially affects the central nervous system. Artificial hydrogen sulfide sources are primarily produced by the processing of crude oil, which has a high content of natural gas and sulfur. H in natural gas₂The concentration of S can be as high as 28%. Artificial discharge is H in the world₂It accounts for about 10% of S emissions. Hydrodesulfurization treatment of oil refinery is H₂It accounts for the majority of S's industrial emissions. H₂Other sources of S's industrial emissions are coke ovens, paper mills, and the leather industry.

H₂Environmental issues related to S-emissions and high-sulfur fuel products (gasoline and diesel) have led to strict government control. These regulations have resulted in significant increases in natural gas and oil processing costs. H₂Several techniques for removing S have been proposed so far.

The most popular method is the Claus process known in the art, thereby H.₂S is converted to sulfur, which is an element, by oxygen combustion. One of the problems with the Claus process is the raw CO₂Is H₂It means that it reacts with S to form carbonyl sulfide and carbon disulfide. Another problem is the unreacted H as an equilibrium point problem.₂It means that S is mixed in the elemental sulfur products. H₂Other methods of removing S include alkanolamines (monoethanolamine, diethanolamine, and methyldiethanolamine), iron / sodium carbonate, thiosarsenate, quinine, and metallic vanadium processes. However, H₂There is still no high-performance, cost-effective, marketable method for removing S from flue gas. H₂Strong cost drivers for S capture are reagent costs (excluding labor costs and construction equipment), treatment and sewage treatment, hardware (absorption vessel, flue gas treatment and plumbing) and installation space constraints.

Providing an efficient and cost-effective hydrogen sulfide removal function is a major technical issue. H₂Various performance areas for improving S capture capability include reducing the vessel size and pressure drop of the reactor and utilizing an efficient mass transfer solvent system that produces commercially available by-products. .. One embodiment of the present invention provides these applicable performances with high H.₂S Achievement with an innovative design method that connects absorption dynamics and value-added production streams.

&lt;Flat jet spray contactor&gt;

The gas-liquid mass transfer process is performed along the gas-liquid interface. The absorption rate of gas into a liquid soap is the liquid phase mass transfer coefficient k._L, Specific surface area (ratio of surface area of gas-liquid interface to volume) a, and bulk fluid C_LAnd gas-liquid interface C_L^*It is controlled by the concentration gradient between and. In many gas-liquid reaction systems, C_L^*Is low in solubility and there is a limit to the control of the concentration gradient. Therefore, in order to increase the gas absorption rate, it is necessary to increase the mass transfer dynamics and increase the ratio of the interface surface area to the volume.

One embodiment of the present invention includes a high performance gas-liquid contactor as described, for example, with reference to FIG. 33. The system can improve overall mass transfer and contactor performance by utilizing a thin flat jet with high density, large surface area and aerodynamic shape. Gas-liquid contactor is about 1 cm^-2About 50 cm from^-2The improved specific surface area, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop of the entire contactor is as low as less than 5 torr / linear ft, and the liquid jet drive pressure. Is characterized by less than 50 psi (more preferably less than 20 psi) and minimal mixing of liquids into the gas stream.

In a preferred embodiment, the system is about 10 cm.^-1About 20 cm from^-1The specific surface area in the range of, the volume of the generator, which is about 1/10 of the volume of the packed bed of the related technology, the pressure drop is as low as less than 1 Torr, the jet drive pressure is about 5 psi, and the gas flow. It includes the feature that the mixing of liquid into the water is minimized.

Gas-liquid contactor is H₂It is available with a variety of conventional liquid (aqueous-based) solvents that oxidize S and other sulfur-based compounds. Oxidizing agents (OX) include water ammonia, alkanolamines (monoethanolamine, diethanolamine, and methyldiethanolamine), iron / sodium carbonate, thiosarsenate, quinine, and metal vanadium processes, sodium hypochlorite. (NaOCl), and hydrogen peroxide (H)₂O₂) Is included, but is not limited to these. Oxidizing agents suitable for use in contacts are basic (pH&gt;) with a catalyst (Cat) that improves the rate of oxidation added as an additive and a stabilizer that controls the decomposition of hydrogen peroxide. 7) Hydrogen peroxide (H₂O₂) It is an aqueous solution. The catalyst additive is, for example, TAML (iron (III) tetra-amide macrocyclic ligand). Stabilizers may be, for example, poly-α-hydroxylacrylic acid, sodium silicate, or dimethylenetriaminepentaacetic acid.

H that can occur when aqueous basic hydrogen peroxide is included₂The chemical mechanism of S oxidation is thought to be as follows. H₂S + OH^- HS^- + H₂O (1) 4H₂O₂ + HS^- SO₄^2- + H⁺ + 4H₂O (2)

&lt;H₂S removal process&gt;

The present embodiment relates to an exhaust gas cleaning process for removing hydrogen sulfide with high efficiency. The present invention includes a nozzle array with a reformed orifice plate (or the nozzle plate described) and a fluid synthesis technique suitable for a wide range of fluids and processing conditions. H₂Removal of S is performed by passing the gas from a high surface through the volumetric gas-liquid contactor unit. Exhaust gas passes horizontally through a gas-liquid contactor, which has a substantially smaller contactor volume and airflow pressure drop than related technologies (referred to as crossflow). Multiple low pressure, vertical flat jet arrays with aqueous sorbents and substantial surface area run across cross currents.

The aerodynamic shape of the flat jet array forms a stable jet flow with less mixing of liquid particles at relatively high gas velocities. Sovent for absorption and removal of sulfur dioxide has a high H₂It has properties such as S capacity, high oxidative stability, low heat of reaction, low solvent cost, low corrosiveness, and a commercially available product stream. An example of Sovent is H₂It is an aqueous solution containing about 10% by weight of hydrogen peroxide and about 0.1% by weight of a catalyst in order to promote the oxidation of S. To optimize the contactor, a suspension of about 1% to about 2% can be added to the aqueous hydrogen peroxide solution to enhance the performance of the contactor. Examples of additives include those that do not react with the aqueous hydrogen peroxide solution and do not interfere with mass transfer. The additive example allows the formation of sorbent properties (eg viscosity) that allow for maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. An example of an additive is bentonite.

Including additional chemical compounds, H₂It is suitable to help the oxidation rate of S and thus mass transfer dynamics. Hydrogen peroxide is an example of an additive to a suitable sorbent system. Stabilizers are added to the sorbent mixture to prevent hydrogen peroxide from decomposing too much at high pH. An example of a hydrogen peroxide stabilizer at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide can be further improved by adding a catalyst of hydrogen peroxide. An example of a hydrogen peroxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

As explained with reference to FIG. 33, this system is H.₂It can be used to remove S. H the process into the gas-liquid chamber 2645₂This will be described by injecting exhaust gas containing S. The gas plenum 2605 evenly distributes gas throughout the liquid flat jet. The liquid jet is generated by pumping the saw vent to the liquid plenum 2635 and spreading the saw vent across the nozzle orifice. The generated jet flows vertically downward into the contact chamber and reaches the capture tank 2620 through the gas-liquid separator. In the gas-liquid chamber 2645, the vertically flowing solvent intersects the crossflow of the gas. Hydrogen sulfide is absorbed by the sorbent liquid and removed from the exhaust stream. The combustion exhaust gas 2655 after cleaning is discharged from the outlet of the contact chamber. The sorbent is recirculated and continuously H from the combustion exhaust stream.₂Remove S.

&lt;CO₂Flat Jet Spray Contactor for Capture Devices&gt;

Another embodiment is CO by utilizing a gas-liquid contactor.₂Regarding the capture of. The gas-liquid mass transfer process is performed along the sea surface of gas-liquid. The absorption rate of gas into a liquid solvent is the liquid phase mass transfer coefficient k._L, Specific surface area (ratio of surface area of gas-liquid interface to volume) a, and bulk fluid C_LAnd gas-liquid interface C_L^*It is controlled by the concentration gradient between and. In many gas-liquid reaction systems, C_L^*Is low in solubility and there is a limit to the control of the concentration gradient. In order to increase the gas absorption rate, the gas-liquid contactor needs to be designed to increase the ratio of mass transfer dynamics, gas-liquid mixing and interfacial surface area to volume.

One embodiment of the present invention relates to a high performance gas-liquid contactor as described above, which utilizes a thin flat jet with high density, large surface area and aerodynamic shape to transfer mass and contactor. It is based on an array that can improve the overall performance of.

One embodiment of the present invention includes a high performance gas-liquid contactor as described, for example, with reference to FIG. 33. The system is based on an array that can improve overall mass transfer and contactor performance by utilizing a thin flat jet with high density, large surface area and aerodynamic shape. Gas-liquid contactor is about 1 cm^-2About 50 cm from^-2The improved specific surface area, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop of the entire contactor is as low as less than 5 torr / linear ft, and the liquid jet drive pressure. Is characterized by less than 50 psi (more preferably less than 20 psi) and minimal mixing of liquids into the gas stream.

In a preferred embodiment, the system is about 10 cm.^-1About 20 cm from^-1The specific surface area in the range of, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop is as low as less than 1 Torr, the liquid jet drive pressure is about 5 psi, and the gas It includes the feature that the entry of liquid into the flow is minimized.

CO₂In order to efficiently capture the contactor, the contactor should be a hindered amine such as monoethanolamine (MEA), methylaminopropanol (AMP) and piperazine (PZ), potassium carbonate (K).₂CO₃) And ammonium hydroxide (usually referred to as aqueous ammonia, with the abbreviation AA), but are available with a wide variety of aqueous-based sorbents. Using a contactor with aqueous ammonia is particularly preferable because it can produce ammonium bicarbonate, convert it to uric acid, which is a fertilizer, or sell it as a chemical raw material, reducing processing costs. CO in ammonia water₂The chemical mechanisms of capture and by-product production are believed to be: 2NH₃ + H₂O + CO₂ (NH₄)₂CO₃ (Ammonium carbonate) (1) (NH₄)₂ CO₃ + CO₂ + H₂O 2NH₄HCO₃ (Ammonium bicarbonate) (2) NH₄HCO₃ + Heat, pressure (NH₂)₂CO (uric acid) (3)

&lt;CO₂Removal process&gt;

The present embodiment is an exhaust gas cleaning process that removes carbon dioxide with high efficiency by the gas-liquid contactor of one embodiment of the present invention. The system has a reformed orifice plate (or nozzle plate) and includes a nozzle array that includes a wide range of fluids and fluid synthesis techniques that suit processing conditions. CO₂Is removed by passing the gas from a large surface through the gas-liquid contact unit, as described above. Exhaust gas passes horizontally through a gas-liquid contactor with a substantially smaller contactor volume and airflow pressure drop (referred to as crossflow). Multiple low pressure, vertical flat jet arrays with an aqueous solvent and substantial surface area run across cross currents. The aerodynamic shape of the flat jet array forms a stable jet flow with less mixing of liquid particles at relatively high gas velocities. Carbon dioxide absorption and removal sources may have properties such as high carbon dioxide capacity, high oxidative stability, low heat of reaction, low solvent cost, low corrosiveness, and a commercially available product stream. Effective CO₂An example of a solvent for removal is an aqueous solution containing 28% by weight of ammonia. To optimize the gas-liquid contactor, about 1% to about 2% polymer or suspension can be added to the aqueous ammonia solution to enhance the contactor performance.

Examples of additives include those that do not react with aqueous ammonia and do not interfere with mass transfer. Suitable polymers or suspensions allow the formation of sorbent properties (eg, viscosity) that allow for maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. Examples of polymer additives include diethylene glycol. Examples of other polymer additives include polyethylene oxide or polyvinyl alcohol. An example of an inorganic additive is bentonite.

As explained with reference to Figure 33, this system is CO.₂It can be used for removal. CO the process into the gas-liquid chamber 2645₂This will be described by injecting exhaust gas containing. The gas plenum 2605 evenly distributes gas throughout the liquid flat jet. The liquid jet is generated by pumping the saw vent to the liquid plenum 2635 and spreading the saw vent across the nozzle orifice. The generated jet flows vertically downward into the contact chamber and reaches the capture tank 2620 through the gas-liquid separator. In the gas-liquid chamber 2645, a vertically flowing sorbent intersects the crossflow of gas. Carbon dioxide is absorbed by the sorbent liquid and removed from the exhaust stream. The exhaust gas 2655 after cleaning is discharged from the outlet of the contact chamber. The sorbent is recirculated and continuously CO from the flue gas stream.₂To remove.

The performance of the gas-liquid contactor is shown on the small subscale testbed in Figure 33. Table 7 summarizes the geometric parameters in this example.<tables num="7"><img id="000009" he="48" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

The configuration of the jet orifice used in this example is as described above. Prior to processing, the surface area of the liquid jet is optimized for jet length, width, and thickness by varying the pump support pressure on the jet orifice plate. Further optimization of jet surface area (length and width) is possible by utilizing additives (eg, diethylene glycol or bentonite) to improve solvent viscosity / surface tension properties, or by remodeling the orifice nozzle.

Table 8 shows an example of the operating conditions and performance of the gas-liquid contactor. Two sorbent systems, aqueous ammonia and MEA, were tested under arbitrary operating conditions. No additives related to viscosity were added to the Sovent mixture. Exhaust gas is air and CO₂But usually CO₂A mixture of gases using a mixture with an air dilution ratio of 1: 9 was injected into a contactor under atmospheric temperature and atmospheric pressure conditions, and measured using a carved mass flow controller. The volumetric flow rate of the liquid was measured by recording the amount of liquid jet discharged into the carved recipient container at the measured time intervals. Reduced (absorbed) CO₂The amount of% CO₂Reduction = 100x (C_in-C_{out out}) / C_in... expressed as (1), where C_inAnd C_{out out}COs in and out of each contactor₂Concentration of. CO in and out of the contactor₂The relative quantity of CO is around 4.2 μm by Fourier transform infrared spectrophotometer (FTIR).₂It is determined by integrating the basic absorption bands of.

Figure 35 shows the CO that turns the jet of liquid ammonia water on and off.₂It is a graph of the FTIR (Fourier transform infrared spectrophotometer) absorption spectrum of. In Figure 35, the average of the four test runs was run for each test result. Background CO₂Concentration of was recorded before each run. CO under the listed test conditions₂Absorption test results are CO₂Was removed at a rate of over 90%. The graph shows CO₂The absorbance of the molecule is 2400 cm^-1From 2250 cm^-1It was the light range of the basic absorption region. From the graph, basic CO₂It clearly shows the reduction of absorptive species in the region, indicating that efficient removal has taken place. By performing a basic mathematical analysis on these spectra, the concentrations that give these absorption levels can be determined, and by examining these proportions, the removal can be shown as a percentage.<tables num="8"><img id="000010" he="73" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;Flat jet spray contactor system for removing gaseous pollutants&gt;

In an embodiment of the invention, a gas-liquid contactor can be used to remove contaminants from the gas stream. The system converts the mass of one phase (gas) into another phase (liquid). In this process, the gas stream is passed through or brought into contact with a liquid spray-shaped or pooled sorbent. As gaseous pollutants dissolve in the sorbent, they are dissolved or absorbed in the liquid sorbent and removed from the gas stream. The extent of the absorption process is governed by mass transfer processing, which includes gas and liquid diffusion, as well as soluble and chemical reactions.

The gas-liquid mass transfer process is performed along the gas-liquid interface. The absorption rate of gas into a liquid solvent is the liquid phase mass transfer coefficient k._L, Specific surface area (ratio of surface area of gas-liquid interface to volume) a, and bulk fluid C_LAnd gas-liquid interface C_L^*It is controlled by the concentration gradient between and. In many gas-liquid reaction systems, C_L^*Due to the low solubility of, there is a limit to the control of the concentration gradient. In order to increase the gas absorption rate, the gas-liquid contactor needs to be designed to increase the ratio of mass transfer dynamics, gas-liquid mixing and interfacial surface area to volume.

One embodiment of the present invention includes a high performance gas-liquid contactor as described herein. The system can improve overall mass transfer and contactor performance by utilizing a thin flat jet with high density, large surface area and aerodynamic shape. Gas-liquid contactor is about 1 cm^-2About 50 cm from^-2The improved specific surface area, the volume of the generator, which is about 1/10 of the volume of the filling tower of the related technology, the pressure drop of the entire contactor is as low as less than 5 torr / linear ft, and the liquid jet drive pressure. Is characterized by less than 50 psi (more preferably less than 20 psi) and minimal mixing of liquids into the gas stream.

In a preferred embodiment, the system is about 10 cm.^-1About 20 cm from^-1The specific surface area of the range, the volume of the generator, which is about 1/10 of the volume of the packed bed of the related technology, the pressure drop is less than 1 Torr, the jet drive pressure is about 5 psi, and to the gas flow. It includes the feature that the mixing of liquid is minimized.

Jet surface area is improved by utilizing various types of aqueous sorbents in combination with polymer additives to capture efficient gas pollutants. H₂S and CO₂Acid gases such as are usually removed with alkanolamines, monoethanolamine (MEA) and diethanolamine (DEA). Basic SO₂And NOx sorbents contain a calcium carbonate mixture (limestone / lime) and ammonium hydroxide (water ammonia), respectively. A customized, all-in-one capture system for the sorbent system is preferred because it simplifies and reduces the size of pollution control contactors. The all-in-one system can be configured in series or in parallel. In addition, the all-in-one system utilizes the gas-liquid contactors described herein.

In a preferred embodiment, the additive that improves the jet surface area is polyvinyl alcohol, polyvinyl oxide, ethylene glycol or diethylene glycol. Inorganic suspensions (eg bentonite) are also suitable for treatments that increase jet surface area. Ammonia water is CO₂, SO₂, NO_xAnd H₂It is a suitable sorbent because it has a function of removing S. By adding an oxidizing agent (for example, hydrogen peroxide), it is possible to help the oxidation of NO and Hg which are difficult to be absorbed in the aqueous solution. Examples of catalysts that activate hydrogen peroxide that operate at high pH include iron (III) tetra-amide macrocyclic ligand (TAML). Preferable examples of hydrogen peroxide stabilizers at high pH include poly (α-hydroxyacrylic acid). Ammonia water is NO for ammonium bicarbonate, ammonium nitrate, and ammonium sulfate_xAnd SO₂Is a particularly suitable solvent because it is produced as a by-product of the reaction with aqueous ammonia. Since these products can be sold as fertilizers, operating costs can be reduced. The basic chemicals for an all-in-one capture and by-product production system are: SO₂capture: NH₃ + H₂O + SO₂ NH₄⁺ + HSO₃^- (1) NH₄⁺ + HSO₃ + NH₃ 2 (NH₄) + SO₃^2- (2) 2H₂O₂ + SO₃^2- H₂O + H₂SO₄ (Sulfuric acid) (3) H₂SO₄ + H₂O 2H⁺ + SO₄^2- + H₂O (4) 2NH₄⁺ + SO₄^2- (NH₄)₂SO₄ (Ammonium sulfate) (5) NO_xcapture: NH₃ + H₂O NH₄⁺ + OH^- (1) H₂O₂ + OH^- HO₂^- + H₂O (2) HO₂^- + NO NO₂ + OH^- (3) NO₂ + NO₂ N₂O₄ (Four) N₂O₄ + H₂O HNO₂ + HNO₃ (Five) HNO₂ + H₂O₂ HNO₃ + H₂O (6) HNO₃ (Aqueous solution) H⁺ + NO₃^- (7) NH₄⁺ + NO₃ (NH₄) NO₃ (Ammonium nitrate) (8) Hg capture: H₂O₂ + Hg⁰ Hg (II) + product (1) H₂S capture: H₂S + H₂O HS^- + H₃O⁺ (1) HS^- + NH₃ + H₂O NH₄HS + OH^- (2)

&lt;System process for gas pollutant removal&gt;

One embodiment of the invention relates to a system comprising a nozzle array for removing gaseous pollutants. The nozzle array has a reformed orifice plate (or nozzle plate) and includes a wide range of fluids and fluid synthesis techniques to suit processing conditions. The removal of pollutant gas is carried out by passing the gas from a high surface through the volumetric gas-liquid contactor unit. Exhaust gas passes horizontally through a gas-liquid contactor with a substantially smaller contactor volume and airflow pressure drop (referred to as crossflow). Multiple low-pressure, vertical flat jet arrays with water-based solvents and substantial surface area run across cross-flow airflows. The aerodynamic shape of the flat jet array forms a stable jet flow with less mixing of liquid particles at relatively high gas velocities.

In a preferred embodiment, a suitable sorbent for gas absorption and removal is high liquid jet performance, high gas loading capacity, high oxidative stability, low heat of reaction, low sorbent cost, low corrosiveness, and commercially available. It is a system with characteristics such as a product stream. As mentioned above, the jet nozzle plate configuration can be optimized in certain embodiments by adding about 1-2% polymer or suspension to the sorbent solution to improve contactor performance.

Examples of suitable additives include those that do not react with the sorbent and do not interfere with mass transfer. Suitable polymers or suspensions allow the formation of sorbent properties (eg, viscosity) that allow for maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. An example of a sorbent would be to contain 28% by weight ammonia and add a polymer additive or suspension to adjust the viscosity of the liquid for optimum jet width, length, and thickness at minimum driving pressure. The increased aqueous solution is raised. An example of a polymer additive is diethylene glycol. An example of an inorganic suspension is bentonite.

The inclusion of additional additives is suitable to aid in the oxidation of contaminants and thus in mass transfer kinetics. Hg is an example of an additive that promotes the oxidation of pollutant molecules.⁰And SO_2、Examples include, but are not limited to, hydrogen peroxide. Stabilizers are added to the sorbent mixture to prevent hydrogen peroxide from decomposing too much at high pH. An example of a hydrogen peroxide stabilizer at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide is further improved by adding a catalyst of hydrogen peroxide. An example of a hydrogen peroxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

In one embodiment, the gas-liquid contactor shown in FIG. 33 can be used to remove pollutant gas. The process is described by injecting the exhaust gas 2600 into the gas-liquid chamber 2465. The gas plenum 2605 evenly distributes gas throughout the liquid flat jet. The liquid jet is generated by pumping the saw vent to the liquid plenum 2635 and spreading the saw vent across the nozzle orifice. The jets generated flow vertically downward into the contact chamber 2645 and reach the capture tank 2620 through the gas-liquid separator 2650. In the gas-liquid chamber 2645, the vertically flowing solvent intersects the crossflow of the gas. The pollutant gas is absorbed by the sorbent liquid and removed from the exhaust stream. The exhaust gas 2655 after cleaning is discharged from the outlet of the contact chamber. The sorbent is recirculated to continuously remove contaminants from the exhaust stream. Table 9 summarizes preferred embodiments of the geometric parameters of this embodiment.<tables num="9"><img id="000011" he="48" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

Prior to processing, the surface area of the liquid jet is optimized for jet length, width, and thickness by varying the pump support pressure on the jet orifice plate. Further optimization of jet surface area (length and width) is possible by utilizing optimal additives to improve the viscosity / surface tension properties of the sorbent, or by reforming the orifice nozzle. However, these tests do not add polymer additives to the liquid sorbent.

Table 10 shows an example of the operating conditions and performance of the gas-liquid contactor. Two sorbent systems, aqueous ammonia and MEA, were tested under arbitrary operating conditions. No additives involved in viscosity or oxidation were added to the Sovent mixture. Exhaust gas is air and CO₂But usually CO₂A mixture with an air dilution ratio of 1: 9 was used. A mixture of gases was injected into the contactor under atmospheric temperature and atmospheric pressure conditions and measured using a carved mass flow controller. The volumetric flow rate of the liquid was measured by recording the amount of liquid jet discharged into the carved recipient container at the measured time intervals. Reduced (absorbed) CO₂The amount of% CO₂Reduction = 100x (C_in-C_{out out}) / C_in... expressed as (1), where C_inAnd C_{out out}COs in and out of each contactor₂Concentration of. CO in and out of the contactor₂The relative quantity of CO is around 4.2 μm by Fourier transform infrared spectrophotometer (FTIR).₂It is determined by integrating the basic absorption bands of. A typical CO that turns on / off a thin flat liquid jet containing liquid ammonia water₂The FTIR absorption spectrum of is shown in FIG. 39. An average of four test runs was run for each test result. Background CO₂Concentration of was recorded before each run. CO under the listed test conditions₂Absorption test results are CO₂Removal rate was over 90%.<tables num="10"><img id="000012" he="69" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;Pilot test in coal combustion power plant&gt;

In this experiment, a trailer-mounted 2 MW unit (10,000 ACFM airflow) was designed and manufactured for pilot testing in a coal-burning power plant. Device systems include gas plenum, flue gas blower, heat exchange submodule, gas-liquid contact module including liquid capture and anti-splash submodule, demister submodule, nozzle array assembly, sorbent pump, liquid treatment submodule, diagnostics and other Consists of attached components. The system is designed to run in a closed-loop stable state or batch configuration to meet the drainage requirements for pollutant-containing sewage in power plants. Early pilot tests were performed on a slipstream on a 0.13 MW scale (nominal value of 650 ACVM combustion emissions) to reduce time and risk. The 650ACFM slipstream was diverted to cleaning equipment using two 6-inch steel pipes. The velocity of the flue gas in the contactor was matched to the velocity of the power plant waste duct (56 ft / s, 17 m / s) using the inlet channel area of 0.2 ft2. The residence time of the gas in the contactor was about 0.04 seconds. When the system was operated with a 5 psi hydraulic drop, a minimum pressure drop of about 0.1 psi was observed in the flue gas. SO₂, NO, NO₂, CO, and CO₂Emissions of flue gas were measured using a flue gas analyzer whose performance was verified by the Environmental Protection Agency (EPA). A slipstream was input to the unit at temperatures and pressures of 150 F and 11.2 psiA. A 0.1 wt% NaOH solution is circulated in the system to SO₂Was washed.

Figure 36 shows a 2 MW prototype system. FIG. 37 shows a gas-liquid contactor. FIG. 38 shows the solvent pump of the system of FIG.

With reference to FIG. 36, the gas-liquid contactor 3210 includes the flat liquid jet contact system described herein. The solvent supply Plenum 3220 provides a solvent that contacts the contactor 3210. In FIG. 37, the combustion exhaust gas enters from the combustion exhaust gas inlet point 3230 and proceeds into the contactor 3210. The combustion exhaust gas goes out from the combustion exhaust gas outlet point 3250. Figure 38 shows the solvent pump 3260. Fig. 39-Fig. 40 is a graph showing the concentration of pollutants that are the target of combustion exhaust gas from coal combustion power plants with and without the Y-axis gas-liquid contactor in relation to the time on the X-axis. .. TESTO₃35 Electrochemical analyzers were used for all three analytical measurements. Figure 39 shows SO in a first small scale test using a contactor in a combustion exhaust gas equivalent of 0.13 MW.₂Indicates the concentration of. When the combustion exhaust gas is activated, SO₂The concentration of was approximately 200 ppm, which reached a substantially stable state. Once you start using the contactor system, these SO₂The emission level of the instrument was immediately reduced to the approximate instrument detection limit and returned to a stable state. The TESTO instrument continues to sample the system even when the contactor is removed, resulting in SO₂It was shown that the concentration rose sharply towards the original contamination level. Figure 40 shows CO when using different sorbents in the same mechanical system.₂It is a figure which shows the level. TESTO analyzer CO₂It clearly shows that the level has decreased and is stable at that level.

Deeper SO₂Efficient CO with removal efficiency (&gt; 99%) meets emission requirements₂It may be necessary for the purpose of pretreating combustion exhaust gas for pollutant removal. Approximately 99.5% SO by using 0.13 MW cleaning equipment₂It is clear from FIG. 39 that the removal efficiency of (average about 99%) was achieved. A scoping test for removing multiple pollutants using approximately 19% by weight ammonia water was also performed as shown in FIG. 40. The system is CO₂Although not optimized for absorption (low, short dwell time), the unit slipstream CO under these conditions.₂Absorbed more than 50% of the amount. In addition, over 99.5% SO₂And more than 80% NO_xWas removed at the same time using aqueous ammonia. 90% CO by jet and medium optimization₂It is expected that only two units will be needed to achieve removal efficiency.

By rapidly scaling and using the results, we were able to demonstrate the operation of an approximately 2 MW (8400 ACFM) modular pilot washer containing a parallel gas-liquid contact module from the same power plant. The inlet channel area of the gas-liquid contactor is approximately 3.9ft²It provides a flow rate consistent with the effluent of a power plant at about 58 ft / s (18 m / s) and a dwell time of about 0.07 seconds. The solvent flow rate is 2800 GPM, providing an L / G of approximately 330 GPM / 1000 ACFM. The jet pressure drop was about 6 psi. The pressure drop across the contact phase of about 2 MW, including the demister and jet filling submodules, was 0.4 psi, where the pressure drop was about 0.1 psi with a jet charge of about 3.3 ft. The input and output combustion exhaust gas temperatures were 250 degrees Fahrenheit and 115 degrees Fahrenheit, respectively. 24-hour test in stable condition (without solvent drainage), mean SO₂The cleaning efficiency was 99%.

Figure 41 shows SO, with a uniform flue gas flow of about 2 MW passing through a larger contactor.₂Shows a large-scale test for capture. Multiple ON / OFF cycles were performed to ensure consistency of operation. Figure 41 shows H₂SO by 2MW scale using O, NaOH (0.1% by weight)₂It is a graph which shows the cleaning result of. The graph shows the time (hours) on the x-axis and the concentration in ppm on the y-axis. SO over 350ppm as shown₂The combustion exhaust gas is discharged as pollutant molecules. The gas-liquid contact module is virtually all SO₂Was removed. More specifically, when the contactor liquid jet was shut off to test if this was reproducible, SO₂The concentration returned to a value above 350 ppm shown in FIG. When you start using the liquid jet module, SO₂The concentration dropped to near the reference value. By repeating this consistently, the same results as shown in FIG. 41 were produced. In addition, recent follow-up tests have led to SO₂The removal efficiency was confirmed. In addition, a simulated sewage treatment experiment using a consumption medium was conducted in the laboratory to prove the precipitation of calcium sulfate.

An embodiment of the present invention is a modular gas-liquid contactor or a plurality of combustion exhaust gas pollutants (SO) under a wide range of combustion exhaust gas conditions._x, NO_x, CO₂And particles) related to gas-liquid contactors, including post-combustion techniques. Wet scrubber systems are susceptible to outages due to mechanical or non-compliance with release rules. The gas-liquid contact cleaning system is designed as a package with a small footprint for continuous online processing with excellent performance, flexibility, convenience and reliability.

Actual performance metrics (eg SO₂Although removal) is directly comparable to traditional methods, equipment design, the process-equivalent designs, methods, and systems of the present invention are less than half the size of traditional systems in achieving these outcomes. It is surprising that the cost is more than 10 times lower than the cost of capital of a conventional system.

A modular design method is used to manufacture and scale modular gas-liquid contact cleaning units. The required pollutant removal performance is achieved by adding cleaning modules in parallel or in series. This is achieved by low pressure drops (eg pressure drops of about 0.4 psi) and low parasitic power requirements (eg less than about 0.8% per step). This method standardizes manufacturing and also allows customization of cleaning equipment for each site requirement. Modular gas-liquid contactors are manufactured in the factory during the assembly line manufacturing process.

&lt;Gas-liquid contact module&gt;

FIG. 42 shows a 60 MW cleaning unit and support structure. FIG. 43 is a front view of one section of the 2 MW section of the scrubber of FIG. 42. FIG. 44 is a side view of one section of the 2 MW section of the scrubber of FIG. 42. FIG. 45 shows the arrangement of the inlet channel and jet filling zone. In this embodiment, the system is configured to have dimensions of less than about 600 lbs and about 5 ftx10 ftx10 ft. These units may also be capable of handling the flow of combustion exhaust gas in excess of approximately 85,000 cfm and can be scaled as appropriate.

The units are designed to be stacked in parallel and sized for the power plant. In some parallel configurations, the modules may be configured on top of each other or next to each other (next to each other). The input gas stream is divided between parallel modules so that each module can perform equal processing (for example, evenly). In one embodiment, 10 2MV base modules are stacked vertically to produce a 20 MW composite module (85,000 cfm). The three 20 MW modules are then connected horizontally to create a 60 MW system so that the input gas stream is evenly divided among the three 20 MW modules, including the 60 MW system.

In this embodiment, as shown in FIG. 42, the sorbent is supplied from the sorbent storage tank 3315 to the solvent supply plenum 3305 of the cleaning system through a plurality of nozzles configured in one nozzle array. The nozzle array primarily provides a planar liquid jet, each liquid jet containing a planar sheet of liquid, with the plurality of liquid jets located substantially in parallel to each other. A flat liquid jet is formed in the scrubber 3345, where the gas stream 3320 passes parallel to the flat surface of the jet. When the sorbent falls to the bottom of the tower, the heat exchanger 3340 captures the heat absorbed by the sorbent during the contact process. The sorbent then flows from within the conduit 3335 into the pump housing 3330, from which more is pumped to the water treatment system 3325.

The water treatment system set forth in 3325 is only schematic and this segment 3325 of the contact system may be small or large, depending on the secondary or tertiary treatment of the liquid. An example of a small system may include only a heat exchanger for diffusing captured gas phase molecules, such as fitting into a "box" in FIG. On the other hand, a large system may include a settling tank, a settling tank, and a solid compression subsystem, which may be large depending on the chemicals utilized and the application.

The pump housing shown in 3330 may be a liquid pump of suitable size for use in supplying a suitable volume of liquid to a contact system known in the art. The block indicated by 3330 is often an option and determines the site environment and pump selection, and whether the selected pump should be provided depending on whether it needs to be protected from rain or snow.

Figures 43-45 show the configuration of the sprayback base unit. The base unit or base module of this embodiment has an input channel of about 25 cm x 130 cm and about 5 sprays / cm based on all 3400 nozzles (40 rows of 85 nozzles) in the spray pack.²Approximately 1.7m including²Consists of a spray pack area. FIG. 43 shows the waste liquid inlet 3360, the waste liquid outlet 3350, and the jet filling zone 3355. The jet filling zone 3355 is the volume of the actual contactor where the liquid jet and gas molecules come into contact with each other. FIG. 45 shows a side cross section of the jet wash filling 3365, followed by a spray or demister 3370 to prevent fluid from entering the waste stream. Even if the liquid jet is fast, some liquid distillation is mixed into the airflow, especially at high gas velocities. The contaminants include small droplets (eg aerosols or mist). The demister contains a small zone in which small mist droplets pass through a zone containing the elements represented by 1660 in Figure 29, which condenses on the surface of these elements and flows back into the liquid tank system. In this particular embodiment, these elements are vertical rods, but can include any design that can cause a small pressure drop and combine condensing / coalescing surfaces with turbulence (eg mesh, heat). Includes, but is not limited to, exchanger elements, or aerodynamic plates or baffles).

FIG. 46 shows a jet filling zone with a removable nozzle plate according to another embodiment of the invention. FIG. 47 shows the configuration of the nozzle plate of the jet filling zone of FIG. FIG. 48 shows the jet filling zone sealing system of FIG. As shown, modular gas-liquid contactors are designed for convenience, accessibility, and reliability. The system (eg, gas-liquid contactor or cleaning unit) has a snap design of the nozzle array, including the orifice plate, which allows the replacement of worn or clogged orifices without interruption. The system can also be designed to have overlapping mechanical equipment or support systems. For example, large plant equipment can include about 20% of the preliminary concept to repair parallel units when needed without interfering with the operation of the plant. Referring to FIG. 46, the partially removed position of the removable plate 3410 is shown. The removable plate 3410 includes a plurality of nozzle plates having multiple rows of nozzles forming multiple parallel flat liquid jets. FIG. 47 shows the entire portion of the removable plate 3410. The removable plate 3415 is shown in the set position and the removable plate 3410 is shown in the removed state. FIG. 48 shows a sealing mechanism 3440 designed to seal the jet plate 3425 against the sealing surface 3435 with an elastomer seal 3430. Illustrated is a side view of a small cross section of the end of the jet plate 3425 and a small enlarged view of the end of a standard jet plate (3410 or 3415). In this embodiment, the jet plate is attached to the 3415, the end of the 3415 having a series of small angled grooves in which the pin 3440 attached to the frame 3435 fits into the groove 3445. .. The angle of the groove 3445 is configured such that the torque generated in the sealing direction causes the angle of the groove to act as a cam with respect to the pin 3440 and pressurize the elastomer seal 3430.

&lt;SO_x, NO_x, And modular gas-liquid contactors in particle processes&gt;

Another embodiment is a Na / Ca dual alkali that includes a compact, high performance, low cost, low water, energy efficient gas-liquid contact system or cleaning system with advanced sewage and product flow treatment capabilities. Deep combustion exhaust gas SO using process₂Regarding the design analyzed for the removal of. The design requirements for this process are shown in Table 11.<tables num="11"><img id="000013" he="106" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;Combustion exhaust gas control system&gt;

A method used in an application for treating combustion exhaust gas using one embodiment of the present invention can be described using general terms. These generalizations can be customized according to the site and usage requirements, but can be divided into four main sections. FIG. 49 is a process flow diagram of the pollutant removal system. In Figure 49, the basic process flow diagram of a gas-liquid contact system shows key system components and key stream points. The four sections are Section 1: Combustion Exhaust Gas or Process Gas Section, Section 2: Cleaning Equipment or Reactor Section, Section 3: Sawvent or Reactor Input, and Section 4: Reactive Biological Treatment and Recycling of Sawvent ( Or release). From the gist of this embodiment, these four sections will be described in detail by taking the use of combustion exhaust gas for desulfurization as an example, but those skilled in the art can make further modifications to these processes to achieve a highly efficient gas-liquid contact system. You will come up with a number of different processes that can benefit from.

With reference to Section 1, the flue gas 5402 is produced and released by industrial treatment (coal-fired power plants, etc.). The flue gas enters section 2 at process point 1 (PP1), the flowing gas is treated in section 2, then passes through PP2, appropriately heated by the optional flue gas heater 5404, and reaches the fan or blower at PP3. Combustion exhaust gas is collected in the combustion exhaust heat stack 5406 with PP4 and prepared for release. Combustion emissions can contain multiple pollutants, depending on the fuel source and the efficiency of combustion. In this embodiment, SO_x, NO_x, H₂O, SO₂, HCl, and HF are the only ones formed in the boiler feeding the reaction system shown in Figure 49. Between the production and release of flue gas 5402, the slipstream (part or all) of this flue gas stream is redirected to pollutant reduction or to the cleaning system (eg Section 2-4).

Section 2 includes a gas-liquid contact modular assembly 5408 that acts as a washer or reactor depending on various embodiments of the invention. In this section, SO when utilizing the chemicals shown in Figure 49₂, HCl, HF, and some NO₂Is removed from the flue gas. CO from this combustion exhaust stream and the chemicals shown in Figure 49₂Efficient removal of is negligible and can improve dramatically depending on the chemicals utilized and the pH of the sorbent, but in this embodiment the CO₂Is rarely captured. Contactor 5408 is SO₂, HCl, and HF. The fluid containing the liquid in the liquid jet is an aqueous solution. This aqueous solution mixed with gas is captured in the capture tank 5410. In Section 2, the captured fluid is recirculated in PP6 with a recirculation pump. The slipstream of this recirculated fluid is drawn using a process valve 5418 to perform the secondary treatment of Section 4.

Section 3 is a fluid section that replenishes the sorbent and solvent, which is configured to regulate the chemical activity, pH of the liquid and replenish the reactants. All liquids lost due to evaporation are replenished with PP7 by a local water source 5412. The liquid is constructed at a relatively high pH (greater than 7) and is maintained at this level at PP8 by the NaOH source 5414, or when the concentration of soluble sulfites reaches a more stable state, in Section 4. The pH can also be maintained by adding lime 5416.

Section 4 describes dissolved or reacted gas phase molecules in a solid product (eg CaSO).₄), Solid filth (eg CaSO)₃), Other available products (eg fertilizer / NH₄SO₄Or NH₄NO₃) Is a secondary treatment section that chemically changes or mineralizes. The process liquid is transported from Section 2 to the settling tank 5420 in PP12 and lime / Ca (OH).₂ 5416 was added with PP15 to raise the pH and Ca²⁺Offer SO₃^2-In (or SO in fully oxidized mode₄^2-(In) Reaction / Precipitation. The resulting CaSO₃The mixture flows into the settling tank 5422 with PP16 and is stored after settling in the slurry holding tank 5424. Sufficient amount of CaSO₃Once captured, it moves to the filter press 5426, where the liquid is removed, passes through PP29 and moves to the salt water retention tank 5428. Solid 5430 from filter press 5426 is processed in a waste disposal facility or CaSO for gypsum / sheet lock for tertiary processes.₄It is sold as. Liquid from salt water tank 5428 is moved in softening step 5432 for recycling or regeneration with PP26 and excess Ca²⁺Removed and soda ash (Na₂CO₃) By adding 5434, Na⁺Is replenished. The regenerated sorbent is sent back to section 2 at PP3 via the secondary process valve 5436.

In a particular embodiment of FIG. 49, a 20 MW system draws some of the flue gas from a 140 MW coal-burning power plant. Combustion emissions are produced by burning low-sulfur coal (eg, from the Powder River Basin, Wyoming). Table 12 shows the specific attributes to be considered in this embodiment. Due to the burning of coal, SO of about 350 to about 400 ppm₂Is produced in the flue gas, which is the main pollutant to be removed in this system example. Other pollutants include HCl, HF, NO_x, And some Hg. This is the front side of Section 1, and the gas flow rate of this slipstream is approximately 84,000 ACFM, as also shown at Process Point 1 (PP1). The temperature of the flue gas coming in at PP1 ranges from about 250 degrees Fahrenheit to about 300 degrees Fahrenheit and comes from the fly ash bag house of an electric power plant. The fly ash bag house serves to remove the bulk fly ash produced from coal combustion and further reduce the temperature to the consistent range described above. The water concentration of this combustion exhaust gas ranges from about 6% to about 8% by mass.

At PP1, the flue gas slipstream enters section 2 (cleaning section). Combustion exhaust gas is about 10m-second for gas-liquid contactor 5404^-1Flows at the gas velocity of. Here, the gas-liquid contactor will be described. The sorbent liquids used are NaOH and SO.₂It is sodium sulfite that is first formed in the initial reaction with. A 50% weight sodium hydroxide solution is added to the water in the sorbent loop to initially bring the pH to approximately 6.5 and maintain this value. NaOH is used during continuous treatment and this pH can be maintained at about 6.5 as appropriate. At start-up, the water is SO₂Can be absorbed to some extent, but this causes the pH value to drop rapidly, resulting in an acidic aqueous solution. Therefore, NaOH keeps the pH approximately neutral and Na⁺SO₃^2-It serves as a counterion for. The following formula is SO₂The main reactions targeted by this system are shown. SO₂ + H₂O 2H⁺ + SO₃^2- (1) 2NaOH + 2H⁺ + SO₃^2- 2Na⁺ + SO₃^2- + 2H₂O (2) During processing in a stable state, this is SO₂It is a sodium sulfite solution that effectively reacts with and has a concentration of about 0.5 M and forms sodium hydrogen sulfite in water by the reaction. The chemical formula representing the entire reaction is as follows. Na₂SO₃ + SO₂ + H₂O 2NaHSO₃ (1)

The flue gas from the contactor is significantly cooled to a temperature in the range of about 100 degrees Fahrenheit to about 125 degrees Fahrenheit by evaporation. A demister downstream of the contactor and inside the module removes excess water. Combustion exhaust gas is SO₂Upon exiting the depleted gas-liquid contactor region (PP2), it may optionally be heated by the combustion exhaust heater 5404 (up to a temperature well above the dew point) and discharged through the ID fan 5440 to the combustion exhaust stack 5406. To. Another option for controlling flue gas is to use the gas to the air heat exchanger to convert it into a wet stack configuration or to use the processed steam of the power plant for reheating. In some cases, the waste heat from the entire sorbent treatment system can also be utilized because it is useful when the hot desorption gas is used in the heat desorption step after leaving the stripper to reheat the combustion exhaust gas. .. Continuous treatment of gas-liquid contactor 5408 led to the construction of sodium bisulfite, SO₂SO unless the reaction product is removed₂Absorption efficiency is reduced. Therefore, the slipstream (PP12) of the liquid sorbent recirculation system of Section 2 is continuously drawn into the secondary chemical treatment system.

In this secondary processing system shown in Section 4, SO₂Is completely mineralized to form a solid product of calcium sulfite (PP16). Calcium sulfite is later filtered (PP18) to remove excess water and properly treated in a waste disposal facility or the like (PP24). Lime (Ca (OH)₂) Serves to mineralize sulfite into a solid precipitate (PP15) and further maintain the pH at appropriate levels as a substitute for additional NaOH additives to the sorbent loop. The reaction performed in the secondary treatment is as follows. 2Ca (OH)₂ + 4NaHSO₃ (CaSO₃)₂H₂O + 2Na₂SO₃ + 3H₂O Calcium scale issues are diverted to the filter press process (PP32) using a standard ion exchange process that utilizes sodium carbonate (soluble in water -PP31) in a later "softening" step (PP26). It can be avoided by removing excess calcium by forming calcium carbonate (which does not dissolve at this pH). In this same step, add sodium thiosulfate (PP34) and sulfite (SO)₃^2-) Sulfate (SO)₄^2-) Can be suppressed. This process is the primary SO₂Capturing reagent Na₂SO₃Also plays a role in regenerating. CaSO₃ + Na₂CO₃ CaCO₃ + Na₂SO₃ After softening and regeneration of the active sorbent chemical, it is recycled back into the main contactor process loop (PP33).

&lt;SO₂And process module removal system&gt;

Process analysis and gas-liquid contactor cleaning and absorption system size are determined based on the design parameters in Table 12.<tables num="12"><img id="000014" he="144" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

The gas-liquid contactor (absorber) is operated in a continuous, stable mode utilizing a cross-popular flat jet spray nozzle. Absorber SO at minimum water, reactor volume, pressure drop, and contact time₂High volume mass transfer (Kca ~ 64s) to maximize removal efficiency^-1) Can be done.

The absorber exhibits a low gas-side pressure drop and a low liquid-side pressure drop that are converted to low power consumption. The pressure drop at the liquid jet orifice is less than about 10 psi, which can significantly reduce the fluid power requirement during operation. A 28,000 gpm liquid pump that circulates the solvent constitutes bulk power consumption within the absorption loop. The power draw P (kW) is ".75 x flow rate (gpm) x ΔP" / "1714 x pump efficiency", about 150 kW for a pressure drop of about 8 psi (or about 20 MWe power draw), about 28,000 gpm. The pump efficiency is about 65%. The pressure drop on the gas side in a flat jet system is as small as about 0.1 psi per 3.3 ft filled jet (2.7 at wc).

In comparison, the average pressure drop of packed towers in related technologies is H for 1 foot packed.₂O is about 1.0 inch, or in a normal 10-foot absorbent bed, H₂O is about 10 inches. Compared to conventional technology, gas-liquid contactors consume less power, and absorbers can operate at higher L / G ratios (330 gallons / 1000 ACFM), thus those of conventional absorbers (L). / G90-130) Higher removal efficiency is achieved.

The absorption system is a target pollutant (eg SO) from the flue gas._x, NO_x, And particulate matter), as well as heavy metals, chlorides, and fluorides. The particulate matter is mostly fly ash carried from baghouses of 2.5 μm or less. Metals and halides are derived from coal and depend on the type of burning coal. All these constituents are removed from the absorption loop of the solvent treatment system. The molar flow from all constituents in the flue gas to the absorption loop is equal to the molar flow of these pollutants in the absorption loop of the solvent treatment system and therefore exits the solid and salt water streams. Concentrations of all constituents in the absorption loop reach a stable state.

Gas solubility, solvent temperature, and pH also play important roles in the absorption of pollutants. The system of this embodiment operates at relatively low liquid temperatures (eg, about 100 to about 125 degrees Fahrenheit) to optimize gas solubility and minimize solvent evaporation. Pollutant gas phase p_aAnd water phase C_aThe solubility of the equilibrium point between (300K) is the Henry's modulus K_H= C_a/ p_aGiven in. SO₂ (g) H₂SO₃, K_H = 1.4M / atm (1) H₂SO₃ H⁺ + HSO₃^-, K₁ = 0.014 M (2) HSO₃^- H⁺ + SO₃^2- , K₂ = 7.1 x 10-8 M (3) HSO₃^- + 1 / 2O₂ SO₄^2- + H⁺ , k&gt; 106 M-1s-1 (4)

For ease of explanation, S (IV) is the sum of all forms of sulfur in the +4 oxidation state ([S (IV)]]._tot= [SO₂] + [HSO^3-] + [SO₃^2-]), And S (VI) is the sum of all sulfur in the +6 oxidation state, [S (VI)]_tot= [SO₃] + [HSO₄^-] + [SO₄^2-]. SO₂Since the gas dissolves in water, the solute is K_H, K₁And K₂Persulfate (HSO) according to the equilibrium point governed by₃^-) And sulfites (SO)₃^2-) Converted to a product. This process is H⁺It depends on the pH when the product is formed. More H⁺When is produced (the pH drops), the equilibrium point shifts back to reactant production. At pH values below 3.5, a significant amount of SO₂Is exhausted from the solvent. SO₂Sodium hydroxide should be added in a stable manner or other chemical bases should be injected into the solvent loop to keep the pH of the system around about 6-7 in order to optimize the removal efficiency and cost of the system. SO_{2 (g)} + 1 / 2O_{2 (g)} + 2 NaOH (aq) Na₂SO₄(aq) + H₂O (1)

&lt;Sulfite oxidation system&gt;

The forced oxidation of sulfites to sulfate can be done in a separate tank (using a 14kW air compressor) with a simple air sparger. Although the sparger is simple, the gas-liquid contact efficiency is low, so the air flow rate is set to about three times the stoichiometric amount required for complete oxidation. Assuming 100% oxidation, about 533 lb / hour of sulfite is oxidized to sulfate. In full-scale systems, the use of additional highly efficient gas-liquid contactors instead of spargers would be cost effective.

&lt;Solvent treatment system&gt;

When the system is run in full oxidation mode (most sulfur and sulphate (SO)₄^2-), The design criteria for sulfate precipitation and removal are shown in Table 13. The system has a &lt;50 ppm HSO in operating liquid in a stable state.₃^-And 14.4% SO₄^2-Designed for. The flow rate of the solvent process stream is SO_xIt is directly dependent on the stable loop concentration of the solvent process system, which determines the size requirements in the design of the solvent process system.<tables num="13"><img id="000015" he="54" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;Advanced design, sorbent, and process options&gt;

Table 14 shows the various solvents, including sodium hydroxide, ammonia, sodium carbonate, magnesium hydroxide, calcium hydroxide, limestone (calcium carbonate), and possibly fly ash. Each sorbent requires a specific sorbent treatment system, and each power generation site may have its own solid and liquid disposal requirements.<tables num="14"><img id="000016" he="114" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

The choice of sorbent / sorbent treatment / disposal system is driven by performance, reagent costs, and site by-product disposal requirements. SO in packed tower with respect to reaction and operating costs₂Table 15 shows the results of comparing the most commonly used reagents for removal.<tables num="15"><img id="000017" he="65" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

Corrosive and ammonia based systems have the highest reactivity and deep SO₂It has the potential for removal, but has the disadvantage of higher costs. The cost of these reactants is significantly offset by the dual loop process, which allows the solvent to be returned to the absorber for recycling. Of all the possibilities, the most promising are NaOH / Ca (OH), NaOH / Ca (OH) and NH / Ca (OH) dual loops. Fly ash has the potential to reduce reagent costs to zero, but carries the greatest risk.

Na / Ca dual loops are preferred, but NH / Ca dual loops are also a possible option. It has the advantages of highly reactive and soluble sorbents, clear contact solutions, and sorbent treatment loops that can recycle relatively expensive ammonia. The advantage of ammonia over sodium is that the precipitation step separates ammonia as a gas so that the return loop is free of calcium and other contaminants that can scale the absorber. In addition, the gas-liquid contact system according to the embodiment of the present invention is CO.₂When combined with an absorption system, ammonia can be used for both purposes. This is because ammonia is volatile and an additional (small) cleaning unit can be placed in the combustion exhaust vent line to prevent the ammonia from slipping onto the stack.

Fly ash has the potential to be used as an FGD absorber due to its alkaline nature and easy availability. Table 16 lists the normal composition of the cooler C fly ash (subbituminous coal). Early attempts to combine FGD with fly ash traps were difficult due to the contaminated downstream of the FGD slurry and its difficult properties to treat. See "Gas Purification" by Kohl et al., Gulf Professional Publishing, 5th Edition, 1997, incorporated herein by reference. However, prepare the fly ash carefully (for example, the best SO)₂-By preventing the reaction of cementum inside the gas-liquid contactor itself (at the CaO / MgO chemistry level), it is possible that the contactor can operate under conditions where the fly ash does not impair the cleaning operation. is there. Alternatively, these C_aA similar reaction of / Mg may be desirable, which can also be used to produce a cementitious material as a commercial product within the sorbent treated area. In addition, if it is desirable to commercialize the by-product gypsum, a solvent treatment system and a disposal scheme that separates fly ash from the gypsum are desired.<tables num="16"><img id="000018" he="75" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;Summary of system&gt;

Na / Ca dual alkaline contact processes and systems have the advantage of higher technical and economic performance than traditional systems. Table 17 summarizes the main basic performance parameters of the contact system and general (per MW) system for the 20 MW of this embodiment.<tables num="17"><img id="000019" he="124" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

Deep SO₂Removal requires fast and efficient mass transfer dynamics, for which NaOH is suitable. Systems utilizing calcium hydroxide / calcium carbonate are low-cost solvents, but they are also low-reaction solvents. Increase reactivity Cooler Im / limestone-based absorbers can be operated on slurries (solids). However, solids are sensitive to the scaling of the absorber surface (due to the formation of calcium sulfite / calcium sulfate) and in some cases further impede mass transfer. The significant cost savings associated with using Na / Ca are due to the re-required sodium (NaOH) in the solvent treatment loop. The operating cost of a dual-loop system is less than that of a single-loop limestone system (especially "gas purification" such as Kohl, incorporated here as a reference, Gulf Professional Publishing, 5th Edition, 1997, as in sulfur-rich fuels. Then). The cheapest reagent is calcium (Ca (OH))₂), Which is used to precipitate gypsum (a by-product of the product). The process advantage of the dual loop system is that it can handle higher sulfur loads, the contact liquid does not corrode, and a fairly efficient gas-liquid contactor can be operated. The disadvantages are the increased complexity and the need for two reagents. In contrast, in the single-loop wet limestone FGD process, all necessary steps are performed in a single container, which is the required step here, in which the limestone is dissolved as calcium carbonate. Make gas-liquid contact and SO₂Is absorbed, reacted with calcium, oxidized and precipitated. The result is a single, relatively simple system. Disadvantages are that the slurry is prone to corrosion / wear, which requires an extraneous nozzle material, and the low efficiency of the spray tower requires a large contact area and thus a large tower.

Table 18 summarizes the parasitic towers for the key equipment components in the contact systems over 20 MW and over 200 MW described here. In these embodiments, it is assumed that the exhaust blower (ID fan) of the combustion exhaust gas cannot be counted because it is already arranged. Connect the bulk power withdrawal to the solvent recirculation pump. The contact system operates from low liquid side fluids and with mechanical stresses due to the large (&gt; 10X of conventional spray nozzle&gt; 10X) flat jet orifice area. In this embodiment, the described 20 MW liquid pump (28,000 GPM) draws significant power from the system with intermediate pump efficiency (~ 65%). It is estimated that a larger liquid pump (&gt; 100,000 GPM) available at full scale operation (&gt; 200 MW) would be significantly more efficient than this (~ 85%), so by using this A fairly low (1.7X) low parasitic power load will be achieved.<tables num="18"><img id="000020" he="72" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;CO₂Process gas-liquid contactor&gt;

These advantages include a compact, low cost, low pressure drop, and high energy efficient cleaning system, CO₂The environmental goals of removal efficiency (&gt; 90%) and energy cost (&lt;20%) were achieved, demonstrating excellence in cost and energy saving process. Three possible absorption / regeneration reactions using ammonia solutions are described in Yeh et al., "Fuel Treatment Techniques," Vol. 86, No. 14-15, pp. 1533-1546, October 2005. Incorporate this as a reference here. 2NH₃_(aq)+ CO_{2 (g)}+ H₂O (NH₄)₂CO_{3 (l)}, Delta H_r= -24.1 kcal / mol (-986 BTU / lb CO₂) (1) NH_{3 (l)} + CO_{2 (g)} + H₂O NH₄HCO_{3 (l)}, Delta H_r = -15.3 kcal / mol (-622 BTU / lb CO)₂) (2) (NH₄)₂CO_{3 (l)} + CO₂+ H₂O 2NH₄HCO_{3 (l)}, Delta H_r = -6.4 kcal / mol (-262 BTU / lb CO₂) (3)

The reaction is exothermic as it has been described for absorption. The most energy efficient CO₂The capture and solvent regeneration method is the carbonic acid / bicarbonate reaction in formula (1). Since it is desirable that the endothermic reaction be carried out at a low temperature, the liquid in the washer is cooled to 90 degrees Fahrenheit and the liquid in the stripper is heated to 140 degrees Fahrenheit to CO.₂Release gas at 1 atm. The use of carbonate / ammonium bicarbonate chemicals can significantly reduce operating costs compared to the use of alkanolamine-based solvents, as the energy produced is less than half that of the EMA.

&lt;Flow diagram and CO of gas-liquid contact process₂Analysis&gt;

FIG. 50 is a process flow diagram from a pollutant removal system in another embodiment . First, the combustion exhaust gas enters the contactor and SO_x, NO_x, And pollutants such as particulate matter are removed. And CO₂Enters the absorber, where it is contacted with, for example, a chilled ammonium carbonate solution or piperazine, and CO₂Most of them are captured as ammonium bicarbonate or as carbamates of piperazine, respectively. Other amines, alkanolamines, and / or bases (eg KOH, NaOH, etc.) are also available in this loop. The chemical system used is an ammonium hydroxide / ammonium carbonate system, in which ammonia from the cooler is mixed into the combustion exhaust gas as ammonia slip, transported to an ammonia cleaning device and removed.

The washed flue gas is transported to a condensate heat exchanger, heated to a temperature above about 40 degrees Fahrenheit above the dew point, and then discharged from the stack. The ammonium carbonate / ammonium bicarbonate absorption stream is recirculated in the chiller and heat pump before being returned to the washer. The sidestream of the absorption solution is removed, overheated and then returned to the stripper to capture the CO.₂To release. The dilute solution returns to the absorption loop. Stripped CO₂Carries some water vapor and ammonia, which are removed during compression in a condensate heat exchanger. Moisture and ammonia are returned to the absorption loop. CO after cleaning₂Is sent to the compression train and quarantined. The main energy-saving process step is to use a heat pump to cool the ammonium carbonate absorption solution and move that heat away from the stripper's solution to raise its temperature and CO.₂Is done by separating. By using a heat pump to capture the energy of the absorption stream and send the heat to the stripper stream, a parasitic power of about 10% can be saved.

Table 20 shows the system size and analytical design criteria. The process is divided into the six main process sections shown in Figure 50, specifically, Section 1 is the flue gas control system and Section 2 is the CO.₂Absorption loop, section 3 is CO₂Stripper loop, section 4 is ammonia or amine slip loop, section 5 is cooling system, section 6 is CO₂It is a compression train. All flow rates and heat loads are calculated for the system shown at 20 MW.<tables num="19"><img id="000021" he="150" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

&lt;Combustion exhaust gas control system&gt;

In this embodiment shown in FIG. 50, the combustion exhaust gas conditioning system includes an inlet 5002 and an outlet 5006 as the combustion exhaust gas enters the optional heat exchanger / cooling device 5004. The flue gas control system already has some treatment (eg SO)₂, HCl, and other acid gas removal treatments). The heat exchanger / cooling device 5004 can be an option (eg, ammonia / ammonia carbonate, as it is known in the art to be dependent on the composition of the incoming gas and the chemistry of the absorber. If so, a cooling device is required). Combustion exhaust gas is cooled and SO₂(For example, in the contact system according to one embodiment of the present invention (not shown)). In this embodiment, the combustion exhaust gas 5002 is CO.₂, N₂, H₂O, O₂, Other pollutants such as rare gases.

&lt;CO₂Absorption loop&gt;

In Section 2, the absorption loop includes a gas-liquid contactor 5008 and a capture tank 5010. The heat exchanger / cooling system 5012 in Section 5 is an optional component. Again, the heat exchanger / cooling device 5012 can be an option as it is known to those skilled in the art that it depends on the composition of the incoming gas and the chemistry of the absorber. In this embodiment, a gas-liquid contactor is connected to outlet 5006 in section 1. The gas-liquid contactor 5008 is connected to the capture tank 5010 and the heat exchanger / cooling device 5012 (section 5) as part of a recycling loop.

In operation, CO₂Direct the flue gas, including, through the inlet 5014 of the gas-liquid contactor 5008, CO₂Separate a part of. Section 2 CO₂Absorption loops include various values and pumps required for proper flow, recycling and operation of liquids known in the art. After contacting the gas with contactor 5008, the absorbed solution will have an additional amount of CO as part of the recirculation loop₂To the capture tank 5010.

In this embodiment, CO₂The energy requirements of the absorption loop are handled by the heat exchanger / cooling device 5012 in Section 5. The general chemistry that utilizes ammonium carbonate, amine, or alkanolamines described here is CO when cooled to a temperature below the temperature of the flue gas found in normal systems.₂Is more preferably absorbed. Therefore, if desired, the heat exchanger / cooling device 5012 of Section 5 can provide cooling functionality to maintain optimal operating conditions for the absorption solution.

&lt;CO₂Stripper loop&gt;

Section 3 includes inlet 5016 connected to heat exchanger / cooling device 5018 with outlet 5020. The outlet 5020 is connected to a gas-liquid contactor 5022. The gas-liquid contactor 5022 has an outlet 5024 connected to a capture tank 5023 with a recycle loop. The gas-liquid contactor 5022 captures CO₂Is configured to be removed from the absorption solution. CO₂Stripping can be done by multiple means (eg, pressure fluctuations, pH regulation, or CO).₂/ Heating of absorption solution). The components in Section 3 can be modified depending on the method selected. In either case, CO₂It is advantageous to capture the absorption solution after release and recirculate the absorption solution to the main absorption loop in Section 2. The output of section 3 is sent to stack 5034.

&lt;NH₃/ PZ absorption loop&gt;

Section 4, which is an ammonia or amine absorption loop, is CO₂Designed to capture ammonia or amine slips from the flue gas exiting the absorber 5008. This process depends on the temperature of the absorption solution (colder means less slip) NH₃It is peculiar when it contains. NH₃The / PZ absorption loop contains a gas-liquid contactor 5026 connected to the inlet 5024. The gas-liquid contactor 5026 includes an outlet 5028, a recycle loop, and an outlet 5032 connected to a capture tank 5030. Implementation of this section can be determined by examining all process requirements and temperature, as there is less need to provide section 4 when using amines such as piperazine or alkanolamines as absorption solutions. This section 4 can be an optional process as there is no need to treat amines with lower molecular weights as they will slip and amines with higher molecular weights will not. Output 5032 may be sent to the flue gas stack 5034.

&lt;CO₂Compression train&gt;

Section 6 is CO₂Shows the process area for stripping from the absorption solution. CO₂The compression train includes a compressor 5036 coupled to a gas-liquid contactor 5022. This section is pure CO from gas-liquid contactor 5022₂Is configured to capture and pressurize. That is, it is desirable to follow this section with secondary oil recovery (EOR), metal ion blockage, and other secondary steps for transport in a convenient way for secondary industrial use. One of these options is CO₂Is compressed with a compression train, isolated at supercritical pressure, and liquid CO₂Can include methods of forming and transporting it to end use by truck or pipeline.

&lt;CO₂Other solvent systems for capture&gt;

In Sections 2 and 3 of Figure 50, various sorbents are CO₂Can be used for capture and / or strip. The sorbent may contain an ammonia carbonate-based solvent of choice as the base solvent. However, the system includes cleaning solvents containing amines such as ammonia, diethanolamine (DEA), and monoethanolamine (MEA), and promoted carbonate, piperazine, tertiary or inhibited amines (methyldiethanolamine (methyldiethanolamine)). It can be done with a variety of post-combustion wet wash solvents, including MDEA) and 2-aminomethylpropanolamine (AMP), metal organic frameworks and molecular encapsulation).

CO₂The embodiment of the system is CO after combustion.₂It presents some of the strengths and benefits of capture. For example, a very large contact surface area becomes available with a small contactor volume. This leads to economic savings in two areas, a small footprint required means a low cost of capital, and a small pressure drop on the liquid side means a low operating cost. It shows that it can be done. Possible CO due to low cost of capital and operating costs₂The range of sorbents is increased. For example, if an inexpensive sorbent has a low reaction rate and requires a large contact area (eg for seawater or deep salt aquifers), CO₂It is still a viable method in gas-liquid contact systems, but will not normally be considered in conventional standard gas-liquid contactors (eg bubble towers or spray towers).

Most mature CO for combustion emissions, alkanolamines and ammonium carbonate / ammonium bicarbonate (AC / ABC)₂In capture systems, maximum energy consumption is associated with heat of reaction. The energy involved in the AC / ABC reaction is CO₂It consumes about 70% of the total energy required for absorption and desorption. ABC solution is CO₂It needs to be cooled to 55 degrees Fahrenheit to absorb it, and it needs to be heated to 265 degrees Fahrenheit to release it to the stripper. The option to achieve energy reduction involves two components. That is, CO₂Find a system with a small heat of reaction during absorption and desorption, or divert the heat released during absorption to the desorption reaction. Ammonium carbonate / ammonium bicarbonate is currently the lowest energy chemical solution. Physical solvents require almost zero renewable energy, but work best at high pressures. Membrane systems can divert absorbed energy to the desorption process, but are currently used only in small systems. Below, CO₂Are classified and described as alternative processes that can be used to capture from flue gas.

Alternative CO₂When looking for an absorption system, the sorbent needs to match the technology used. We have developed three post-combustion absorption technologies: gas-liquid contactors, dry contact systems, and membrane contact systems. The gas-liquid contact system requires a liquid saw vent. The gas-liquid system divides absorption and desorption into two separate process steps, performed in two separate containers at different pressures and temperatures. This system typically costs energy in both the steps of cooling for endothermic absorption and heating for endothermic absorption. This process requires varying temperature and / or pressure and requires a lot of energy. A dry regenerative sorbent system using sodium bicarbonate is the same process as a gas-liquid contactor, except that the sorbent is in solid phase.

However, the membrane system is basically different. The membrane of the membrane system is a very thin partition wall made of a permeable material that separates the two streams and may be a solid or liquid held by a sponge-like material. The membrane is designed to select the gas to separate. Regardless of whether the material of the membrane is solid or liquid, the membrane is CO on the concentrated side.₂Absorb, CO₂Move to the dilution side where is desorbed. The driving force is CO over a very thin film₂Concentration gradient of. The aesthetic of the membrane system is that absorption and desorption can be performed in the same container, at the same temperature, and at almost the same pressure. Since the absorption and desorption take place within a few microns of each other in a very thin membrane, the absorbed energy can be transferred to the desorption reaction at a constant temperature. Therefore, the change in entropy is zero, and the required net energy is also zero. The liquid in the membrane is selectively CO₂You can choose what you can carry. Disadvantages are manufacturing costs, membrane life, very clean flue gas requirements, and huge contact areas (approximately one million square meters for the entire commercial system). 100m²Combustion exhaust gas of hundreds of thousands of ACFM that enters the duct up to the cross section of each fiber has a cross-sectional area of 60 nm.²Need to channel to billions of fibers.

Alternative solvent systems available for post-combustion absorption in gas-liquid contactors include chemical and physical ones. Wet chemical sources include amines, carbonates, accelerators, hybrids, and pH fluctuations. Wet physical sorbents include metal-organic frameworks, ionic liquids, seawater, and underground saline. Glycol is a high pressure system and is not described as it is more suitable for pre-combustion absorption. SELEXOL is an example of a commercial glycol system currently used for cleaning natural gas and is a high pressure process. CO₂Each wet sorbent available for gas-liquid contactors will be described below.

Hydrous amines are CO of power plants recognized by those skilled in the art.₂This is the current state of the art for capture. Amine sorbent is ammonia (NH₃), Monoethanolamine (MEA), Methyldiethanolamine (MDEA), 2-Minomethylpropanolamine (AMP), PZ Piperazine (PZ), etc. All first CO₂In response to (CO₂ + 2RNH₂ RNH₂COO RNHCOOH), produces amine carbamate. In addition, amines and water are CO₂Reacts with to produce amine bicarbonate (RNH)₂ + H₂O + CO₂ RNH₃⁺ + HCO₃^-). Absorption / desorption can be performed by the lowest energy reaction (bicarbonatecarbonate). All amine systems require gas-liquid contactors and strippers. The system described here is suitable in that it is a very efficient gas-liquid contactor. Although any amine system has advantages, ammonia is cheaper and the reaction energy of ammonia is lower than that of alkanolamines such as MEA, so carbonate / ammonium bicarbonate sorbent was selected.

Alkaline carbonates include Na, K, and Ca, carbonates / bicarbonates. Alkaline carbonates were introduced to ambient temperature and CO in the early 1900s.₂It was used primarily for the purpose of pressure absorption, but has recently been superseded by the more efficient alkanolamines. CO₂Since the rate of absorption of water into an aqueous solution is usually slow, an accelerator (catalyst or enzyme) is often added to increase the rate.

Examples of accelerators include "gas purification" such as Kohl, incorporated herein by reference, Formaldehyde, MEA, DEA, glycine, and carbonic anhydrase described in Gulf Professional Publishing, 5th Edition, 1997. .. CO₂The fastest catalyst available for absorption is an enzyme called carbonic anhydrase (incorporated here for reference, MC Trachtenberg, L Bao, SL Goldman, etc., 2004, 7th International Conference on Greenhouse Gas Control Technology (GHGT-7). ), Vancouver, BC). Amino acids are also COs equivalent to or greater than MEA or DEA₂Jacco van Holst, Patricia.P.Politiek, John PMNiederer, Geert F. Versteeg, etc. CO₂It is described in "Capture" and is incorporated here as a reference. Enzymes and catalysts do not change the reaction energy or change its equilibrium point, but they do reduce the activation energy and increase the reaction rate on the order of a few magnitudes. CO in water₂Hydrolysis and subsequent reaction to bicarbonate is very slow. The effect of increasing the speed is to reduce the required contact area by reducing the residence time required for contact. However, because it is a biological enzyme, CA is sensitive to temperature and cannot be used for temperature fluctuation processes performed at high desorption temperatures. This means that we have no choice but to utilize the pressure fluctuation process. CO in combustion exhaust gas₂Partial pressure is about 0.15 atm, so pure CO₂The total pressure of desorption should be less than approximately 0.1 atm when capturing. Another candidate for CA is to pressurize all combustion emissions before contact. Other accelerators (such as DEA) are currently used in hot potassium carbonate processes at high temperatures and pressures.

The hybrid sorbent uses a combination of sorbent sandwich and amine. The example currently used is K₂CO₃/ PZ, which is an aqueous potassium carbonate solution in which piperazine (PZ), which is expected to consume less energy than MEA, is used as an accelerator. This system is currently being studied at the University of Texas at Austin. CO₂Absorption rate and load are K from MEA₂CO₃/ PZ is significantly larger. In addition, PZ loss and degradation is significantly less than MEA, by Plasynski et al., "Capturing Carbon Dioxide by Absorption by Potassium Carbonate, Carbonation Isolation, Overall Project", USDOE, NETL, April (2008). As described in. The main contribution of the GLC absorber to this system is the effect that capital and operating costs are achieved by increasing contact efficiency, reducing footprint and reducing pressure drop.

The last chemical absorption / desorption system described is pH variation, which is not usually mentioned due to the very high energy costs. CO₂Is absorbed by base-like NaOH and released by acid-like HCl. The resulting salt is electrolyzed to regenerate acids and bases. Energy inputs are used electrochemically rather than pressure or temperature fluctuations. The calculated energy requirement is much higher than that of other processes. Still this process is SO₂It has been commercialized for absorption purposes. Physical sorbents include glycols, metal-organic frameworks (MOFs), ionic liquids, seawater, and underground salt water. These utilize physical absorption rather than a chemical reaction with sorbent. Energy is not involved in the chemical reaction, but the desorption process requires a pressure change.

CO with 700psi syngas₂Glycol works best at high temperatures, which are used in pressure fluctuation processes (such as the selexol process) that have been proposed as a process of separating before combustion. Gas-liquid contact systems are not available for high pressure absorption processes.

Metal-Organic Framework (MOF) is CO₂A "cage" of molecules that contains small bubbles of gas. MOF is highly selective, has excellent absorption / desorption rate, and has high CO₂It has a capacity and can be used for gas-liquid contactors and liquid membranes. However, the risk is the high reagent cost and the fact that it has not been used in gas-liquid contactors.

An ionic liquid is an organic salt that is liquid at room temperature, not an aqueous solution. Ionic liquid is CO₂And SO₂Since it absorbs both of these, it is expected to be used for cleaning combustion exhaust gas. It can be used for gas-liquid contactors and liquid membranes. Like MOF, ionic liquids can only be synthesized on a laboratory scale, which can result in very high reagent costs. Moreover, it has never been tested with a gas-liquid contactor.

For underground salt water or seawater, CO₂Since the preferred method of isolation is injection into deep salt aquifers, potential methods for both capture and isolation are CO.₂Is absorbed in natural alkaline underground salt water and reinjected into the solution. As a result, CO to be injected as a gas₂No energy is required to desorb and compress. Depending on the alkalinity of the groundwater, the absorption rate may be slow and a large contact area may be required. A very large surface area of the GLC contactor is the perfect solution. In addition, although many naturally occurring saline aquifers are rich in Ca and / Mg, groundwater alkalinity may need to be enhanced by lime, which is optimal for capital and operating costs. Trade-off relationships need to be taken into account.

This process is basically unlimited absorption and disposal (although it depends on the site, of course) CO₂Or SO₂Similar to either / both seawater absorption. In addition, seawater is naturally abundant in Ca and Mg, which can easily form solid precipitates as carbonates or sulfates. This proportion or other desired proportion can also be artificially produced utilizing various magnesium and / or calcium salts such as nitrates, hydroxides, sulfates, carbonates, or halides. The solubility of these salts varies dramatically depending on the starting compound, pH, and temperature of the target solution, so those skilled in the art need to take into account their purpose and the compound of interest.

The table below shows the various COs available for gas-liquid contactors.₂It compares the advantages, disadvantages, and estimated costs between sorbent systems.<tables num="20"><img id="000022" he="195" wi="159" file="JP5777215B2_D0001.tif" img-format="tif" img-content="drawing" /></tables>

Various modifications and variations to the present invention will be apparent to those skilled in the art without departing from the scope and spirit of the present invention. Accordingly, the present invention is intended to include modifications and variations of the invention that occur within the scope of the claims and their equivalents.<u style="single">(Item 1)</u><u style="single"> Liquid inlet and</u><u style="single"> Gas inlet and</u><u style="single"> Gas outlet and</u><u style="single"> A nozzle array that communicates with the liquid inlet and the gas inlet to generate a plurality of flat liquid jets at uniform intervals having a shape that minimizes disturbance from the gas.</u><u style="single"> A gas-liquid separator that allows liquids to pass through while substantially blocking the passage of gases,</u><u style="single"> A liquid outlet that communicates with the gas-liquid separator,</u><u style="single"> A gas-liquid contact module equipped with.</u><u style="single">(Item 2)</u><u style="single"> The module according to item 1, further comprising at least two gas-liquid contact modules connected in parallel.</u><u style="single">(Item 3)</u><u style="single"> The module according to item 1, further comprising at least two gas-liquid contact modules connected in series.</u><u style="single">(Item 4)</u><u style="single"> The module according to item 1, wherein the gas-liquid contact module includes a material selected from the group consisting of copper, nickel, chromium, steel, aluminum, a coating metal, and a combination thereof.</u><u style="single">(Item 5)</u><u style="single"> The above-mentioned gas-liquid contact module is the module according to item 1, which includes a plastic material.</u><u style="single">(Item 6)</u><u style="single"> The module according to item 1, wherein the gas-liquid contact module includes at least one of a structural polymer, a polyimide, a composite thereof, and a combination thereof.</u><u style="single">(Item 7)</u><u style="single"> The module according to item 1, wherein the nozzle array includes a plurality of nozzles having a staggered configuration.</u><u style="single">(Item 8)</u><u style="single"> The module according to item 1, wherein the gas-liquid contact module has a size for processing an increment of the entire predetermined processing requirement.</u><u style="single">(Item 9)</u><u style="single"> The module according to item 1, wherein the nozzle array is oriented to provide a cross-flow gas-liquid contact module.</u><u style="single">(Item 10)</u><u style="single"> The module according to item 1, wherein the nozzle array is oriented to provide a parallel flow gas-liquid contact module.</u><u style="single">(Item 11)</u><u style="single"> The module according to item 1, wherein the nozzle array is oriented to provide a backflow gas-liquid contact module.</u><u style="single">(Item 12)</u><u style="single"> The module according to item 1, wherein the nozzle array includes at least two nozzles separated by a distance of more than about 0.2 cm.</u><u style="single">(Item 13)</u><u style="single"> The module according to item 1, wherein the nozzle array contains at least one row of nozzles.</u><u style="single">(Item 14)</u><u style="single"> The module according to item 1, wherein the nozzle array contains at least three rows of nozzles separated by a uniform distance.</u><u style="single">(Item 15)</u><u style="single"> The module according to item 1, wherein the nozzle array includes a U-shaped channel.</u><u style="single">(Item 16)</u><u style="single"> The module according to item 1 in which the nozzle array includes a V-shaped channel.</u><u style="single">(Item 17)</u><u style="single"> The module according to item 1, wherein the nozzle array includes a channel having a depth of more than about 2 mm.</u><u style="single">(Item 18)</u><u style="single"> The module according to item 1, wherein the nozzle array includes channels having a depth in the range of about 2 mm to about 20 mm.</u><u style="single">(Item 19)</u><u style="single"> The module according to item 1, wherein the liquid inlet supplies liquid to the nozzle array at an angle of about 90 degrees with respect to the nozzle channel.</u><u style="single">(Item 20)</u><u style="single"> The nozzle array includes a first row nozzle, a second row nozzle, and a third row nozzle, and the second row nozzle is the first row nozzle and the third row nozzle. Item 1. The module according to item 1, which is provided between the nozzles of the first row and the nozzles of the second row are offset from the nozzles of the first row and the nozzles of the third row.</u><u style="single">(Item 21)</u><u style="single"> The module according to item 1, wherein the nozzle array includes at least one nozzle in which the ratio of the minor axis to the major axis is less than 0.5.</u><u style="single">(Item 22)</u><u style="single"> The nozzle array is about 0.25 mm</u>^{<u style="single">2</u>}<u style="single">From about 20mm</u>^{<u style="single">2</u>}<u style="single">The module according to item 1, which comprises at least one nozzle having a projected cross-sectional area in the range of.</u><u style="single">(Item 23)</u><u style="single"> The above-mentioned gas-liquid separator is the module according to item 1, which substantially minimizes the back splash of liquid during operation.</u><u style="single">(Item 24)</u><u style="single"> The above-mentioned gas-liquid separator is the module according to item 1, which includes a plurality of components.</u><u style="single">(Item 25)</u><u style="single"> The module according to item 24, wherein the plurality of components include a plurality of curved vane pumps spaced apart from each other.</u><u style="single">(Item 26)</u><u style="single"> The module according to item 24, wherein the plurality of components include a plurality of angled vane pumps spaced apart from each other.</u><u style="single">(Item 27)</u><u style="single"> The module according to item 1, further comprising a liquid drain plenum provided adjacent to the gas-liquid separator.</u><u style="single">(Item 28)</u><u style="single"> 27. The module according to item 27, further comprising a demister that removes at least a portion of the liquid that enters the gas.</u><u style="single">(Item 29)</u><u style="single"> The demister is the module according to item 28, which includes a plurality of baffles.</u><u style="single">(Item 30)</u><u style="single"> The module according to item 28, wherein the demister is provided adjacent to the gas outlet.</u><u style="single">(Item 31)</u><u style="single"> The module according to item 1, wherein the liquid flat jet contains at least one of water, ammonia, ammonia salt, amine, alkanolamine, alkali salt, alkaline earth salt, peroxide, and hypochlorite.</u><u style="single">(Item 32)</u><u style="single"> The module according to item 1, wherein the liquid flat jet contains at least one of a calcium salt aqueous solution and a magnesium salt aqueous solution.</u><u style="single">(Item 33)</u><u style="single"> The above liquid flat jet is the module described in item 1 including seawater.</u><u style="single">(Item 34)</u><u style="single"> The module according to item 1 in which the above liquid inlet contains salt water.</u><u style="single">(Item 35)</u><u style="single"> A method of processing gas-phase molecules with a gas-liquid contactor.</u><u style="single"> The stage of forming a plurality of essentially planar liquid jets, each containing a planar liquid sheet, each of which is configured on a substantially parallel plane.</u><u style="single"> The step of supplying a gas containing at least one reactive or soluble gas phase molecule, and</u><u style="single"> A step of removing at least a part of the gas phase molecule by mass transfer interaction between the gas phase molecule and the plurality of liquid jets.</u><u style="single"> How to prepare.</u><u style="single">(Item 36)</u><u style="single"> The interaction due to the above mass transfer is about 1 second.</u>^{<u style="single">-1</u>}<u style="single">About 250 seconds from</u>^{<u style="single">-1</u>}<u style="single">35. The method of item 35, which has a volume mass transfer coefficient in the range of.</u><u style="single">(Item 37)</u><u style="single"> The interaction due to the above mass transfer takes about 5 seconds.</u>^{<u style="single">-1</u>}<u style="single">About 150 seconds from</u>^{<u style="single">-1</u>}<u style="single">35. The method of item 35, which has a volume mass transfer coefficient in the range of.</u><u style="single">(Item 38)</u><u style="single"> The interaction due to the above mass transfer takes about 10 seconds.</u>^{<u style="single">-1</u>}<u style="single">About 100 seconds from</u>^{<u style="single">-1</u>}<u style="single">35. The method of item 35, which has a volume mass transfer coefficient in the range of.</u><u style="single">(Item 39)</u><u style="single"> The stage of supplying the above gas is</u><u style="single"> The ratio of gas flow rate to the volume of the reaction chamber is about 100 minutes</u>^{<u style="single">-1</u>}<u style="single">About 1000 minutes from</u>^{<u style="single">-1</u>}<u style="single">35. The method of item 35, which comprises a step of supplying a gas that is in the range of.</u><u style="single">(Item 40)</u><u style="single"> The step of forming an array of the plurality of flat liquid jets with uniform spacing is</u><u style="single"> 35. The method of item 35, which comprises the step of forming the flat liquid jet at a hydraulic pressure in the range of about 2 psig to about 50 psig.</u><u style="single">(Item 41)</u><u style="single"> The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a width greater than about 1 cm.</u><u style="single">(Item 42)</u><u style="single"> 35. The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a width ranging from about 1 cm to about 15 cm.</u><u style="single">(Item 43)</u><u style="single"> 35. The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a thickness in the range of about 10 μm to about 1000 μm.</u><u style="single">(Item 44)</u><u style="single"> 35. The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a thickness in the range of about 10 μm to about 250 μm.</u><u style="single">(Item 45)</u><u style="single"> 35. The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a thickness in the range of about 10 μm to about 100 μm.</u><u style="single">(Item 46)</u><u style="single"> 35. The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a length in the range of about 5 cm to about 30 cm.</u><u style="single">(Item 47)</u><u style="single"> 35. The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a length in the range of about 5 cm to about 20 cm.</u><u style="single">(Item 48)</u><u style="single"> The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a speed of less than 15 m / sec.</u><u style="single">(Item 49)</u><u style="single"> The method of item 35, wherein at least one of the plurality of flat liquid jets in the array has a velocity in the range of about 5 m / sec to about 15 m / sec.</u><u style="single">(Item 50)</u><u style="single"> Method of removing gas phase molecules with the device of item 1.</u><u style="single">(Item 51)</u><u style="single"> The method according to item 50, wherein the gas phase molecule comprises at least one of sulfur oxides, nitrogen oxides, carbon dioxide, ammonia, acid gas, amines, halogens, and oxygen.</u><u style="single">(Item 52)</u><u style="single"> The method according to item 50, wherein the gas phase molecule contains a sulfur oxide.</u><u style="single">(Item 53)</u><u style="single"> The method according to item 50, wherein the gas phase molecule contains carbon dioxide.</u><u style="single">(Item 54)</u><u style="single"> The method according to item 50, wherein the gas phase molecule contains nitrogen oxides.</u><u style="single">(Item 55)</u><u style="single"> The method according to item 50, wherein the gas phase molecule contains an amine.</u><u style="single">(Item 56)</u><u style="single"> The method according to item 50, wherein the gas phase molecule contains chlorine.</u><u style="single">(Item 57)</u><u style="single"> Item 35, wherein the planar liquid jets include at least one of water, ammonia, ammonia salts, amines, alkanolamines, alkali salts, alkaline earth salts, peroxides, and hypochlorites. The method described.</u><u style="single">(Item 58)</u><u style="single"> The method according to item 35, wherein the plurality of planar liquid jets include at least one of a calcium salt aqueous solution and a magnesium salt aqueous solution.</u><u style="single">(Item 59)</u><u style="single"> The method according to item 35, wherein the plurality of planar liquid jets include seawater.</u><u style="single">(Item 60)</u><u style="single"> The method according to item 35, wherein the plurality of planar liquid jets contain salt water.</u><u style="single">(Item 61)</u><u style="single"> With the reaction chamber</u><u style="single"> With the gas inlet connected to the reaction chamber,</u><u style="single"> With the gas outlet connected to the reaction chamber,</u><u style="single"> With the liquid plenum connected to the reaction chamber,</u><u style="single"> A nozzle array connected to the liquid plenum, each containing a planar liquid sheet, each providing a plurality of essentially planar liquid jets configured on substantially parallel planes.</u><u style="single"> With the gas-fluid separator connected to the reaction chamber,</u><u style="single"> A gas-liquid contact system equipped with.</u><u style="single">(Item 62)</u><u style="single"> 61. The system of item 61, further comprising a secondary chemical treatment subsystem that is in fluid contact with the liquid plenum.</u><u style="single">(Item 63)</u><u style="single"> The subsystem according to item 61, wherein the gas-liquid contact system mineralizes absorbed sulfur oxides into a sulphate or sulfate.</u><u style="single">(Item 64)</u><u style="single"> The above gas-liquid contact system absorbs CO</u>_{<u style="single">2</u>}<u style="single">61. The subsystem according to item 61.</u><u style="single">(Item 65)</u><u style="single"> The above gas-liquid contact system is pure CO</u>_{<u style="single">2</u>}<u style="single">61. The subsystem according to item 61.</u><u style="single">(Item 66)</u><u style="single"> The subsystem according to item 61, wherein the gas-liquid contact system reacts absorbed nitrogen oxides into soluble nitrates.</u><u style="single">(Item 67)</u><u style="single"> The system of item 61, further comprising a demister provided at the gas outlet.</u><u style="single">(Item 68)</u><u style="single"> 67. The system of item 67, further comprising a gas outlet plenum connected to the gas outlet.</u><u style="single">(Item 69)</u><u style="single"> 68. The system of item 68, further comprising a capture tank for fluid communication with the reaction chamber.</u><u style="single">(Item 70)</u><u style="single"> The system according to item 61, wherein the nozzle array includes a plurality of nozzles in a staggered configuration.</u><u style="single">(Item 71)</u><u style="single"> The system of item 61, wherein the nozzle array is oriented to provide a cross-flow gas-liquid contact system.</u><u style="single">(Item 72)</u><u style="single"> The system of item 61, wherein the nozzle array is oriented to provide a parallel flow gas-liquid contact system.</u><u style="single">(Item 73)</u><u style="single"> The system of item 61, wherein the nozzle array is oriented to provide a backflow gas-liquid contact system.</u><u style="single">(Item 74)</u><u style="single"> The system of item 61, wherein the nozzle array comprises at least one row of nozzles.</u><u style="single">(Item 75)</u><u style="single"> The system according to item 61, wherein the nozzle array includes a U-shaped channel.</u><u style="single">(Item 76)</u><u style="single"> The system according to item 61, wherein the nozzle array includes a V-shaped channel.</u><u style="single">(Item 77)</u><u style="single"> The system of item 61, wherein the nozzle array includes channels having a depth greater than about 2 mm.</u><u style="single">(Item 78)</u><u style="single"> The system of item 61, wherein the nozzle array includes channels having a depth in the range of about 2 mm to about 20 mm.</u><u style="single">(Item 79)</u><u style="single"> The system of item 61, wherein the nozzle array comprises at least one nozzle in which the ratio of the minor axis to the major axis is less than 0.5.</u><u style="single">(Item 80)</u><u style="single"> The nozzle array is about 0.25 mm</u>^{<u style="single">2</u>}<u style="single">From about 20mm</u>^{<u style="single">2</u>}<u style="single">61. The system of item 61, which comprises at least one nozzle having a projected cross-sectional area in the range of.</u><u style="single">(Item 81)</u><u style="single"> It s a gas-liquid contactor,</u><u style="single"> With the fluid plenum that supplies the contact liquid,</u><u style="single"> A contact chamber that communicates with the fluid plenum and receives the contact liquid from the fluid plenum,</u><u style="single"> A gas inlet that communicates with the contact chamber,</u><u style="single"> A gas outlet that communicates with the contact chamber,</u><u style="single"> With</u><u style="single"> The gas-liquid contactor system described above takes about 5 seconds.</u>^{<u style="single">-1</u>}<u style="single">About 250 seconds from</u>^{<u style="single">-1</u>}<u style="single">A gas-liquid contactor that interacts by mass transfer with a volume mass transfer coefficient in the range of.</u><u style="single">(Item 82)</u><u style="single"> The gas-liquid contactor of item 81 further comprising a nozzle array.</u><u style="single">(Item 83)</u><u style="single"> The gas-liquid contactor of item 81, wherein the nozzle array comprises at least one row of nozzles.</u><u style="single">(Item 84)</u><u style="single"> The gas-liquid contactor according to item 81, wherein the nozzle array includes a U-shaped channel.</u><u style="single">(Item 85)</u><u style="single"> The gas-liquid contactor according to item 81, wherein the nozzle array includes a V-shaped channel.</u><u style="single">(Item 86)</u><u style="single"> The gas-liquid contactor according to item 81, wherein the nozzle array includes a channel having a depth of more than about 2 mm.</u><u style="single">(Item 87)</u><u style="single"> The volume mass transfer coefficient is about 10 seconds.</u>^{<u style="single">-1</u>}<u style="single">About 100 seconds from</u>^{<u style="single">-1</u>}<u style="single">The gas-liquid contactor according to item 81, which is in the range of.</u><u style="single">(Item 88)</u><u style="single"> The volume mass transfer coefficient is about 5 seconds.</u>^{<u style="single">-1</u>}<u style="single">About 25 seconds from</u>^{<u style="single">-1</u>}<u style="single">The gas-liquid contactor according to item 81, which is in the range of.</u><u style="single">(Item 89)</u><u style="single"> A gas-phase molecular treatment system with multiple modular gas-liquid contactors arranged in parallel or in series so that they can be sized according to the gas-phase molecular treatment.</u><u style="single">(Item 90)</u><u style="single"> Item 89, wherein each of the plurality of modular gas-liquid contactors includes a nozzle array that essentially provides a plurality of planar liquid jets, each of the plurality of liquid jets comprising a planar liquid sheet. System.</u><u style="single">(Item 91)</u><u style="single"> The method according to item 50, wherein the vapor phase molecule contains a volatile organic compound.</u>