JP5777215B2 - Gas-liquid contactor and exhaust cleaning system and method - Google Patents

Description

  The present invention is a continuation of “Two,” which is a continuation of US patent application Ser. No. 11 / 057,539 (currently No. 7,379,487) filed February 14, 2005 under the name “Two Phase Reactor”. This is a continuation-in-part of US Patent Application No. 12 / 012,568 filed February 4, 2008 under the name “Phase Reactor”, and named “System for Gaseous Pollutant Removal” on September 26, 2008. US Provisional Application No. 61 / 100,564, filed September 26, 2008, entitled “Liquid Gas Contactor System and Method”, “Liquid Gas Contactor System and Method” We claim the benefit of US Provisional Application No. 61 / 100,591, filed September 26, 2008 under the name “Contactor and Effluent Cleaning System and Method,” the entire disclosure of which is incorporated herein by reference. No.

  The present invention relates to gas-liquid contactors and exhaust cleaning systems and methods, and more particularly, to maximize the interaction between air and liquid while minimizing disturbance from gas and liquid during high-speed replenishment of liquid. The present invention relates to a nozzle array that generates a plurality of uniformly spaced flat liquid jets having shapes that can be made.

  Absorption of gases into liquids is an important process step in various gas-liquid contact systems. Airflow contactors, also known as gas-liquid reactors, are classified as surface reactors and volume reactors, where an interfacial surface area between two phases is formed in the liquid surface and bulk liquid, respectively. There are many examples of surface gas-liquid reactors such as rotating disks and liquid jet contactors. A rotating disk generator is a disk (rotor) that is partially immersed in a liquid and exposed to an air stream. A thin film of solution is formed on the surface of the rotor and is in contact with a cocurrent flow of reagent. The disc is rotated to renew the contact of the liquid reagent with the gas. In the volume type gas-liquid reactor, the gas phase is dispersed as fine bubbles in the bulk liquid. The shape of the bubble may be spherical or irregular, and is introduced into the liquid by a gas sparger. Bubbles can be mechanically disturbed to facilitate mass transfer.

ここで変数Φは反応装置の単位体積あたりの気体吸収率（モル／ｃｍ^３）であり、φは単位界面積あたりの平均吸収率であり（モル／ｃｍ^２）であり、ａは、単位体積あたりの気液界面積（ｃｍ^２／ｃｍ^３、またはｃｍ^−１）であり、ｐおよびｐｉは、バルクガスおよび界面における試薬気体の分圧（バール）であり、Ｃ_Ｌ ^＊は、既存の気相濃度ｐｉで均衡点となるような液体側の濃度（モル／ｃｍ^３）であり、Ｃ_Ｌ（モル／ｃｍ^３）はバルク液体の溶解気体濃度の平均値であり、ｋ_Ｇおよびｋ_Ｌは、それぞれ気体側および液体側の質量移動係数（ｃｍ／ｓ）である。 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, the interface surface area A, and the concentration gradient ΔC between the bulk fluid and the gas-liquid interface. Therefore, the general form of the absorption rate of the gas into the liquid is expressed as follows.

Here, the variable Φ is the gas absorption rate per unit volume of the reactor (mol / cm ³ ), φ is the average absorption rate per unit interface area (mol / cm ² ), and a is the unit volume. Gas-liquid interfacial area (cm ² / cm ³ , or cm ⁻¹ ), p and pi are the partial pressure (bar) of the reagent gas at the bulk gas and the interface, and C _L ^* is the existing gas phase The concentration on the liquid side (mole / cm ³ ) is the equilibrium point at the concentration pi, C _L (mole / cm ³ ) is the average value of the dissolved gas concentration of the bulk liquid, and k _G and k _L are The mass transfer coefficients (cm / s) on the gas side and liquid side, respectively.

In the related art, there are many ways to maximize mass transfer and specific surface area in a gas contactor system. The main methods include gas sparger, wet wall jet method, spraying method or atomization. Which gas-liquid contactor is selected is determined according to reaction conditions such as air / liquid flow, mass transfer, and the nature of the chemical reaction. Table 1 summarizes various mass transfer characteristics of gas-liquid reactors in some related art. In order to optimize the gas absorption rate, it is necessary to maximize the parameters k _L , a, and (C _L ^* −C _L ). In many gas-liquid reaction systems, the control of the concentration gradient is limited because the solubility of C _L ^* is very low. Thus, the primary parameters in designing an efficient gas-liquid flow reactor are mass transfer and the ratio of interfacial surface area to reactor volume (also known as specific surface area).

There are many gas-liquid contact devices whose characteristics depend on the interface contact area. For example, a chemical oxygen iodine laser (COIL) generates laser energy from a chemical fuel consisting of chlorine gas (Cl ₂ ) and basic hydrogen peroxide (BHP). This reaction results in singlet delta oxygen that powers COIL. This technique utilizes a circular jet of liquid BHP mixed with Cl ₂ gas to produce this singlet delta oxygen. In a typical generator, the jet has a diameter on the order of 350 microns or less. In order to generate a jet, liquid BHP is pressed with pressure by a nozzle plate having a high density and containing holes. This increases the interfacial surface area in contact with the Cl ₂ gas. The larger the surface area, the smaller the generator and the higher the yield of excited oxygen that can be supplied to the laser cavity. Smaller, more densely packed jets increase specific surface area, but are also prone to clogging and breakage. Clogging is important because the reaction of chlorine with basic hydrogen peroxide produces a chlorine salt of an alkali metal hydroxide that is used to produce basic hydrogen peroxide. It is a problem. Further, the clogging limits the molar concentration range of basic hydrogen peroxide, reducing singlet oxygen yield and laser power. The heaviest element in the COIL system is this chemical fuel. Problems inherent in fuel production increase the overall weight of the COIL laser and reduce efficiency. Accordingly, it is desirable to provide a COIL laser that is more efficient and less weight than current designs.

As another example, gas-liquid contactors are also used for aerobic fermentation processes. One of the most important reagents in this aerobic fermentation is oxygen. Its solubility in aqueous solution is low, but it needs to be high to maintain the culture. In a commercially available fermenter (> 10,000 L), the bubble dispersion is agitated to increase the volume mass transfer coefficient k _La . By stirring, the dissolved oxygen moves through the bulk fluid, destroying the coalescence of bubbles and reducing the boundary layer surrounding the bubbles. The interfacial area in these systems can be increased by increasing the number of bubbles in the reactor and reducing the bubble diameter. However, the oxygen mass transfer of microorganisms is still constrained by the relatively small interfacial surface area of the bubbles and short bubble residence times. In the current sparger system (bubble dispersion), the volume mass transfer coefficient k _La is relatively small at about 0.2 / s, so that a maximum interfacial surface area can be generated and a new one that can overcome these mass transfer restrictions There is a desire for a method.

  The design of industrially available systems needs to take into account both cost and efficiency. None of the conventional methods generally satisfy these two aspects. For example, industrial applications of conventional gas-liquid contactors require gas phase chemicals to react or dissolve with the liquid phase in chemical processing, industrial biological applications, pollution control, or dynamic flow systems. It was decided to be similar processing.

  Taking pollution control as an example, a standard method for removing target compound (s) by wet processing is a reverse flow that uses small droplets of a liquid phase that falls 180 degrees opposite to the flowing gas phase. System. Usually, gravity is used to introduce a liquid phase into a capture sump at the tower or base of the tower. The gas phase flows through the same tower or tower. This gas phase is then captured and further processed or released to the atmosphere.

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

  Another disadvantage of standard backflow systems is that the velocity of the airflow needs to be slow enough so that the gravitational effect is greater than the buoyancy of the droplet in a gravity or spray / droplet gas-liquid contactor. is there. Regardless of the fact that most of the liquid reagent evaporates due to the long contact time, it is necessary to capture most of this water vapor before secondary processing or release.

  Accordingly, the present invention is directed to a gas-liquid contactor and exhaust cleaning system and method that can substantially eliminate one or more problems due to limitations and disadvantages existing in the related art.

  One advantage of the present invention is that it provides a large volumetric mass transfer coefficient and thus enables a small low pressure sorbent process with minimal pumping capability required throughout the system.

  Another advantage of the present invention is that it can provide a gas-liquid contactor with a smaller system footprint than 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 improving the specific surface area of a 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, there is less cost and site impact than conventional systems with the same reaction and wash capacity, potentially between quality and unit There is a possibility that it can be kept highly consistent.

  Other features and advantages of the invention will be set forth in the description which follows, and in part will be apparent from the description, and may be learned when the invention is practiced. The objectives and other advantages of the invention may be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended 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 in communication with the liquid inlet and the gas inlet. The nozzle array produces a plurality of uniformly spaced flat liquid jets having a shape that minimizes disturbance from the airflow. The gas-liquid separator allows the liquid to pass while substantially preventing the passage of the gas. The liquid outlet is in fluid communication with the gas-liquid separator.

  Another embodiment of the invention relates to a method of processing gas phase molecules in a gas-liquid contactor. The method includes forming a plurality of essentially planar liquid jets, each including a planar liquid sheet, each configured on a substantially parallel plane. The method further includes providing a gas comprising at least one reactive or soluble gas phase molecule, and interacting at least a portion of the gas phase molecule with mass transfer between the gas phase molecule and the plurality of liquid jets. Removing or reacting with each other.

  Yet another embodiment of the 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 is coupled to a liquid plenum and provides a plurality of essentially planar liquid jets that each include a planar liquid sheet, each configured on a substantially parallel plane. The system further comprises a gas fluid separator coupled to the reaction chamber.

Yet another embodiment of the present invention relates to a gas-liquid contactor. The gas liquid contactor includes a fluid plenum for supplying contact liquid and a contact chamber in communication with the fluid plenum for receiving contact liquid from the fluid plenum. The gas inlet and outlet are in communication with the contact chamber. Gas-liquid contactor systems interact by mass transfer having a volumetric mass transfer coefficient in the range of about 5 sec- ¹ to about 250 sec- ¹ .

  Yet another embodiment of the invention relates to a gas phase molecular processing system. The gas phase molecular processing system includes a plurality of modular gas-liquid contactors arranged in parallel or in series so as to 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 (for example, a thin flat liquid jet) having an increased specific surface area. 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 opposed planar walls attached to the apex of the V-shaped chamber. A flat jet nozzle may include a conical nozzle mounted as a V-shaped chamber at the opposite end of an opposing planar wall. In another configuration, the orifice of the jet may include a circular orifice attached to the liquid source chamber. The flat jet nozzle may include 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, opposite or parallel to the gas source inlet. The minimum passage of the flat jet nozzle may be greater than about 250 μm. The nozzle may produce a liquid flat jet whose width is at least 10 times greater than its thickness. The flat jet may be thin, such as a thickness of 10 μm or less, separated by a spacing greater than or less than 1 mm, with a high filling jet density (β = 0.01), a large specific surface area (approximately 20 cm ^{− 1} ) can be achieved. This is a significant improvement of about 5 to about 10 times the specific surface area values found in Table 1. The thin jet exposes more liquid to the air stream, resulting in a higher yield of reaction products per unit liquid mass flow than conventional contactors.

  Another embodiment of the present invention has an orifice that has a large specific surface area, a uniform jet velocity, a shape that can minimize gas turbulence in the liquid jet, and does not cause salt damage or clogging. And providing a gas-liquid contactor that produces a plurality of closely spaced, thin, flat jet streams that operate within a cross-flow, co-current, counter-flow, and parallel flow gas treatment stream.

  Yet another embodiment of the invention relates to an improved COIL. The COIL includes an excited oxygen generation chamber having an inlet for a chlorine source and a flat jet nozzle for a 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 generation chamber has a passage connected to the excitation oxygen generation chamber and an inlet for iodine. The BHP orifice may produce a basic hydrogen peroxide flat jet having a width at least 10 times its thickness. The hydrogen peroxide source may be basic hydrogen peroxide utilizing a single base or multiple 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 coupled to a first end of a pair of parallel and opposing plates.

  Yet 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. An improved COIL that includes an excited oxygen generation chamber. The hydrogen peroxide in this embodiment is a gas. The nozzle has a minimum dimension of a length greater than about 600 μM and produces a thin flat jet with a large specific surface area. The photon generation chamber has a passage connected to the excitation oxygen generation chamber and an inlet for iodine.

Another embodiment of the present invention, oxygen, CO _2, and other nutrients or feed gas, and, according to the fermentation reactor with improved includes a nozzle containing a plurality of orifices to produce a flat jet of the fermentation medium.

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

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

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 in communication with the fluid plenum and receiving contact liquid from the fluid plenum. The gas-liquid contactor further includes a gas inlet that communicates with the contact chamber and supplies gas, and a gas outlet that communicates with the contact chamber and carries gas to the outside. Further, the gas-liquid contactor is characterized by a specific surface area ranging between about 1 cm ⁻¹ and about 50 cm ⁻¹ and a pressure drop of less than about 5 Torr.

Another feature may be that the specific surface area ranges between about 10 cm ⁻¹ and about 20 cm ⁻¹ . 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 coal-fired power plant output reactor passing through a reactor volume less than about 15 cubic feet per minute and per mole output (MW) of plant output. Some are greater than about 2500 cubic feet in actuality, or the ratio of gas flow rate to reaction chamber volume ranges from 100 min ⁻¹ to 1000 min ⁻¹ . Another feature is that the liquid drive 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 about 99% of the liquid is eliminated. 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 jet generates a plurality of parallel jet rows. There is something. Another feature is that the gas flows in the contact chamber parallel to the rows of jets.

Another embodiment of the invention relates to a method of contacting a gas with a liquid. The method includes providing a gas-liquid contactor that includes a fluid plenum for supplying contact liquid, and providing a contact chamber in communication with the fluid plenum and receiving contact liquid from the fluid plenum. The contact chamber includes a gas inlet that communicates with the contact chamber and provides a gas, and a gas outlet that communicates with the contact chamber and carries the gas to the outside. The gas-liquid contactor is characterized by a specific surface area ranging between about 1 cm ⁻¹ and about 50 cm ⁻¹ . The gas is driven with a pressure drop of less than about 0.05 psi for one linear foot of air in the contactor.

Another feature is that the specific surface area ranges between about 10 cm ⁻¹ and about 20 cm ⁻¹ . Another feature relates to a method of driving contact liquid into a contact chamber at a pressure of less than about 20 pounds per square inch. Another feature is that about 99% of the liquid is eliminated. 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 such that the nozzles generate a plurality of parallel jet rows. There is. Another feature is that the gas flows in the contact chamber parallel to the jet sheet.

  Another embodiment of the invention relates to a gas-liquid contactor comprising a plurality of essentially planar liquid jets, each of these plurality of liquid jets comprising a planar liquid sheet, wherein these plurality of liquids. The jets are arranged on parallel planes. A contact chamber containing a plurality of planar liquid jets has an input and an output defining a gas flow. One feature is that the thickness of the planar 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. Another feature may be a thickness in the range of about 10 μm to about 50 μm. Another feature is that each planar liquid sheet is separated from adjacent planar sheets 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 includes a plurality of nozzles that generate a plurality of liquid jets, although other geometric configurations may be utilized. Another feature is that each of the plurality of nozzles has a substantially elliptical outlet. As another feature, a plurality of nozzles may be disposed on a single plate. As another feature, a plurality of nozzles may be arranged on the plate to allow gas to flow parallel to the flat surface of the flat liquid jet. As another feature, the plurality of nozzles may be arranged as a plurality of rows forming a nozzle array and a liquid jet. As another feature, the gas-liquid contact module may include an anti-splash grid. As another feature, the anti-splash grid members may be angled to assist in the flow of liquid after passing through the contact chamber. As another feature, the gas-liquid contact module may include a demister.

  Yet another embodiment of the invention relates to a nozzle that produces a flat liquid jet, which may include a plate that houses the nozzle. Embodiments further include a nozzle fluid inlet hole having a V-shaped cross section and a nozzle fluid outlet hole having a conical outlet in cross section. One feature is that the narrowest hole of the fluid outlet hole engages with the narrowest hole of the fluid outlet hole to form the narrowest hole of the nozzle. Another feature is that the narrowest hole of 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 present invention relates to a plurality of nozzles that produce a thin flat liquid jet that includes a substantially V-shaped channel and forms fluid inlet holes for the plurality of nozzles. Embodiments further include 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 may be that the conical cross section and the narrowest hole of the plurality of nozzles is larger than 600 μm.

  Yet another embodiment of the present 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, the plurality of flat liquid jets may be parallel to the flue gas flow. As another feature, a plurality of flat liquid jets may be arranged in rows. As another feature, the system may include a flue gas cooler. As another feature, the system may include a flue gas heater. As another feature, the system may include a second cleaning unit. As another feature, the cleaning unit may comprise a gas-liquid fluid separator. As another feature, the system may include a solvent pump that pumps solvent to the wash unit and a plurality of nozzles. As another feature, the system may include a solvent capture tank that collects the solvent that has passed through the wash unit. As another feature, the plurality of nozzle plates may be removable from the cleaning unit.

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

  Yet another embodiment of the invention relates to a method of contacting a liquid with a gas. The method provides a contact chamber that includes a liquid inlet point that forms a plurality of flat liquid jets in the contact chamber and forms a gas flow parallel to the plurality of flat liquid jets. One feature is that the liquid entry point includes a plate containing a plurality of 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 outlet in cross section. As another feature, the method may further configure the plurality of liquid jets as a plurality of rows.

Yet another embodiment of the present invention includes a fluid plenum for supplying contact liquid, a contact chamber in communication with the fluid plenum for receiving contact liquid from the fluid plenum, and a gas inlet in communication with the contact chamber for supplying gas. And a gas-liquid contactor having a gas outlet communicating with the contact chamber and carrying gas to the outside. The specific surface area of the contact chamber ranges from about 10 cm ⁻¹ to about 20 cm ⁻¹ and the volume mass transfer coefficient on the liquid side of the contact chamber is greater than about 0.02 cm / s. As one feature, the liquid side mass transfer coefficient is greater than about 0.1 cm / s. As another feature, the liquid side mass transfer coefficient is greater than about 1 cm / s. As another feature, the liquid side mass transfer coefficient is greater than about 10 cm / s. As another feature, the liquid side mass transfer coefficient is greater than about 25 cm / s. Another feature is that the liquid side mass transfer coefficient is about 50 cm / s or less.

Another embodiment includes a fluid plenum for supplying contact liquid, a contact chamber in communication with the fluid plenum for receiving contact liquid from the fluid plenum, a gas inlet in communication with the contact chamber for supplying gas, and a contact chamber The present invention relates to a gas-liquid contactor having a gas outlet communicating and carrying gas to the outside. The specific surface area ranges between about 10 cm ⁻¹ to about 20 cm ⁻¹ and the 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 sec −1. Another feature is that the volume mass transfer coefficient is greater than about 10 seconds −1. Another feature is that the volume mass transfer coefficient is greater than about 100 sec-1. Another feature is that the volume mass transfer coefficient is greater than about 1000 sec-1. Another feature is that the volume mass transfer coefficient is less than about 2500 sec-1.

  Yet another embodiment relates to a gas-liquid contactor that includes a fluid plenum for supplying contact liquid. The contactor further includes a plurality of nozzles in fluid communication with a fluid plenum that generates a plurality of flat liquid jets. The contactor includes a chamber in communication with the fluid plenum and receiving contact liquid from the fluid plenum via a plurality of nozzles. The gas inlet communicates with the contact chamber to supply gas, and the gas outlet communicates with the contact chamber and carries the gas to the outside. As one feature, 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. Another feature is that the jet length 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 velocity of the plurality of flat liquid jets is about 10 m / s.

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 in communication with the fluid plenum and receiving contact liquid from the fluid plenum. The gas inlet communicates with the contact chamber to supply gas, and the gas outlet communicates with the contact chamber and carries the gas to the outside. Gas-liquid contactors are characterized by an improved specific surface area ranging between about 1 cm ⁻¹ and about 50 cm ⁻¹ and a very low pressure drop of less than about 5 Torr (or 1 psig). As another feature, this very low pressure drop is less than about 0.05 psi for the contact distance of a linear gas-liquid contactor. As another feature, this very low pressure drop is less than about 1 psi for the entire gas-liquid contact system including gas heaters, gas coolers, and demisters. Another feature is that the contact liquid is arranged by a plurality of nozzles that generate a flat liquid jet when the liquid flows through the plurality of nozzles, the plurality of nozzles being arranged to form a plurality of parallel jet rows Has been. Another feature is that the gas flows in the contact chamber parallel to the jet rows.

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 in communication with the fluid plenum and receiving contact liquid from the fluid plenum. The gas inlet communicates with the contact chamber to supply gas, and the gas outlet communicates with the contact chamber to carry the gas to the outside. The gas-liquid contactor is characterized by an improved specific surface area ranging between about 1 cm ⁻¹ and about 50 cm ^{−1 and} the liquid driving pressure for placing the contact liquid in the contact chamber is less than about 15 psi. One feature is that the liquid drive pressure that places the contact liquid in the contact chamber is 10 psi. Another feature is that the contact liquid is arranged by a plurality of nozzles that generate a flat liquid jet as the liquid flows through the plurality of nozzles, the plurality of nozzles arranged so that the jet forms a plurality of jet rows Has been. Another feature is that the gas flows in the contact chamber parallel to the jet rows.

Yet another embodiment of the present invention relates to a high performance gas-liquid contact module. The module includes a fluid plenum that supplies a 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 gas, and the gas outlet communicates with the contact chamber to carry the gas to the outside. The gas-liquid contactor is characterized in that the contaminant removal rate is a value greater than about 80% in percentage. One feature is that the contactor volume is less than about 0.5 m3. Another feature is that the contaminant removal rate is greater than about 90% as a percentage. Another feature is that the contaminant removal rate is greater than about 95%. Another feature is that the contaminant removal rate is about 99% as a percentage. Another feature is that a plurality of modular gas-liquid contactors are designed to be arranged in parallel so that the integrated system can be sized as required. Another feature is that a plurality of 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 system parasitic load may be less than about 5%. Another feature is that the system parasitic load may be less than about 1%. As another feature, the cleaning removal rate of contaminants such as SO ₂ may be greater than about 90% in percentage. Another feature is that the cleaning removal rate of contaminants such as SO ₂ may be greater than about 95%. As another feature, the cleaning removal rate of contaminants such as SO ₂ may be greater than about 99% in 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 a reactive or soluble liquid to the contact module. In addition, it includes gas inlets and outlets that provide a conduit for the reactive gas or gas solute or gas phase reactant to pass through the contact module. The supply of fluid through the contactor is performed by a nozzle array in liquid communication with the liquid inlet, the nozzle array having a uniform spacing with a shape that can minimize disturbance from the gas flowing through the contactor. Producing a plurality of flat liquid jets. A gas-liquid separator is disposed across the contactor chamber from the liquid jet nozzles to allow liquid to pass while substantially preventing gas from passing through, and is in liquid contact with the liquid outlet.

  Another embodiment of the invention relates to a method of processing gas phase molecules in a gas-liquid contactor. The method includes a plurality of liquid jets that are basically planar, each including a planar liquid sheet. Each of the plurality of liquid jets is configured on a substantially parallel plane. The method further comprises supplying a gas comprising at least one reactive or soluble gas phase molecule, wherein at least one of the gas phase molecules is due to an interaction by mass transfer between the gas phase molecule and the plurality of liquid jets. 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 A gas fluid separator coupled to the reaction chamber. The nozzle array provides a basically planar liquid jet. Further, each liquid jet includes a planar liquid sheet, which are arranged as a plurality of liquid jets that are each basically arranged in a substantially parallel plane.

Another embodiment of the invention relates to a gas-liquid contactor in which a fluid plenum supplies contact liquid to the contact chamber. The second feature is that the contact chamber is in communication with the fluid plenum and receives itself from the fluid plenum. A third feature is that the contactor has a gas inlet and a gas outlet in communication with the contact chamber. Overall, the gas-liquid contact system interacts by mass transfer having a volumetric mass transfer coefficient in the range of about 1 sec- ¹ to about 250 sec- ¹ .

  It is to be understood that the foregoing general description and the following detailed description are exemplary and explanatory and are intended to provide further explanation of the claimed invention.

  The accompanying drawings are included to provide a further understanding of the invention, and are included and constitute a part of this specification, illustrating embodiments of the invention, and illustrating the principles of the invention together with the description. To play a role.

  The following is a brief description of the drawings.

It is a block diagram of the system which produces | generates the flat jet in one Embodiment of this invention.

It is a block diagram of the system which produces | generates the excitation oxygen in another embodiment of this invention.

FIG. 6 is a block diagram of an improved chemical oxygen iodine laser in another embodiment of the present invention.

It is an upper surface right perspective view of the flat jet nozzle in another embodiment of the present invention.

FIG. 5 is a bottom left perspective view of the flat jet nozzle of FIG. 4.

FIG. 6 is a cross-sectional view of a nozzle bank precursor in another embodiment of the present invention.

It is a side view of the precursor of the nozzle bank shown in FIG.

It is a top view of the nozzle bank in another embodiment of the present invention.

It is a side view of the nozzle bank of FIG.

FIG. 9 is a cross-sectional view of the nozzle bank of FIG. 8 cut along B of FIG. 9.

FIG. 9 is a diagram illustrating in detail the nozzle bank of FIG. 8 defined by cutting in FIG. 9A.

FIG. 9 is a perspective view of the nozzle bank of FIG. 8.

It is a perspective view of the board which welds a nozzle bank.

It is a side view of the nozzle plate in another embodiment of the present invention.

It is a top view of the nozzle plate of FIG.

FIG. 15 is a perspective view of the nozzle plate of FIG. 14.

FIG. 16 is a detailed exploded view of the nozzle plate of FIG. 14 cut at A shown in FIG. 15.

FIG. 15 is a perspective view of an array of flat and thin flat liquid jets produced by the nozzle plate of FIG. 14.

FIG. 15 is a front view of an array of flat and thin flat liquid jets produced by the nozzle plate of FIG. 14.

FIG. 15 is a side view of an array of flat and thin flat liquid jets produced by the nozzle plate of FIG. 14.

Fig. 5 shows a fluid outlet side of a nozzle plate in another embodiment of the invention.

FIG. 22 shows a fluid inlet side of the nozzle plate of FIG. 21.

Fig. 5 shows a fluid outlet side of a nozzle plate of another embodiment of the present invention.

24 shows the fluid inlet side of the nozzle plate of FIG.

Fig. 4 shows the fluid outlet side of the nozzle plate with the nozzle bank removed.

FIG. 26 shows a fluid inlet side of the nozzle plate of FIG. 25.

It is a top view of the precursor of a nozzle bank.

It is a side view of the precursor of FIG.

It is a schematic cutaway view of the gas-liquid contactor in another embodiment of the present invention.

The schematic arrangement | positioning of the several gas-liquid contactor in another embodiment of this invention is shown.

FIG. 5 is a schematic diagram of a multiple contaminant removal system in another embodiment of the present invention.

FIG. 5 is a schematic diagram of a multiple contaminant removal system in another embodiment of the present invention.

FIG. 3 is a schematic view of a general gas-liquid contactor that generates an interaction between a gas phase and a liquid phase in another embodiment of the present invention.

FIG. 6 is a graph showing the relationship between the NO ₂ removal system absorbency and runtime. FIG.

_CO 2 FTIR (Fourier transform spectrophotometer) which jets aqueous ammonia liquid is ON / OFF is a graph of the absorption spectrum.

A system of a 2 MW prototype is shown.

A gas-liquid contactor is shown.

42 shows a solvent pump of the system of FIG.

H ₂ O, is a graph showing the cleaning results of SO ₂ by 0.13MW scale utilizing NaOH (0.1 wt%).

19 is a graph showing the cleaning results of the CO ₂ by 0.13MW scale utilizing wt% aqueous ammonia.

H ₂ O, is a graph showing the cleaning results of SO ₂ by 2MW scale utilizing NaOH (0.1 wt%).

Represents a 60 MW cleaning unit and support structure.

FIG. 43 is a front view of a section of the 2 MW section of the wash tower of FIG. 42.

FIG. 43 is a side view of a section of the 2 MW section of the wash tower of FIG. 42.

The arrangement of the inlet channel and jet filling zone is shown.

1 represents a jet filling zone having a removable nozzle plate.

The structure of the nozzle plate of the jet filling zone of FIG. 46 is shown.

FIG. 47 shows the jet filling zone sealing system of FIG. 46. FIG.

FIG. 6 is a process flow diagram of a contaminant removal system in another embodiment of the present invention.

FIG. 6 is a process flow diagram from a contaminant removal system in another embodiment.

  The present invention relates to a gas-liquid contactor and an exhaust cleaning system and method, and more particularly, to a nozzle array that generates a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbance from a gas. Related. In addition, various embodiments provide multiple small single unit processes integrated in a module, and these designs overcome the disadvantages of conventional designs. By modularizing single unit processing, the system can be scaled to scale by simply multiplying the module by a convenient integer to expand the small system.

  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 take place within a very small airflow rate design. Is much smaller than the conventional back-flow reactor in the yield of the equivalent reactor. Integration into one or more modules may be done either in series or in parallel.

  In the serial embodiment, the modules are combined one by one with the gas flowing through each module sequentially. Of course, some modules have loops that are bypassed or recirculated. Furthermore, the modules may be run in the same liquid phase or in different liquid phases depending on the desired selectivity of the reaction to be captured and sequenced for gas molecules.

  In a parallel embodiment, the modules are included next to each other or on top of each other so that all processing or cleaning of the same gas supply occurs, and where each module is a gas or gas that is substantially equivalent to the adjacent module. Treat with molecular weight. In general, parallel modules perform in the same liquid phase since processing for each is performed simultaneously with that of adjacent modules.

  One embodiment of the present invention aims to accommodate higher airflow rates or smaller mass transfer coefficients than this single module design standard, the module itself being multiplied by a convenient integer unit, Can be made a larger functional module with a longer contact time without dividing the system into multiple overlapping systems. In addition, this design logic may be extended to other sub-modules of the chemical processor (eg, liquid capture system and liquid delivery system), 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 air and / or liquid flow systems) can be scaled linearly to provide increased modules, and the unique design of these modules can be linked together. This forms a functionally single process in a very compact design.

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

  In another embodiment of the present invention, the gas-liquid contactor is selective for gas reactants and has a high mass transfer rate from a high volume gas flow rate to a continuously filled gas constrained to a small system volume. Configured to achieve a flow rate of Further, the various methods of the present invention allow a large, dense, packed, high speed, stable liquid jet (eg, a thin flat liquid jet) to interact with a high speed air stream. The orifice and density forming the jet can be optimized based on the liquid solvent or reaction characteristics such as viscosity and surface tension. In general, if the chamber size or the entire process scale is not taken into account, increasing the liquid viscosity will improve the stability of the liquid jet. Accordingly, the nozzle density of the nozzle array increases as the nozzle size decreases. This is not essential, but may be desirable for purposes of reducing jet-to-jet spacing and increasing and optimizing contactor specific surface area. In contrast, low surface energy tends to destabilize the jet, leading to the formation of small droplets in some conditions, which is undesirable in the present invention, but is commonly seen in the current state of the art. It is done. In the case of low surface energy, it may be possible to optimize the jet characteristics for any fluid by lowering the hydraulic pressure and increasing the nozzle size.

  In one embodiment of the present invention, the efficiency of processing gaseous and liquid reactants is increased compared to conventional methods and systems. The efficiency of the method and system is achieved by low pressure solvent processing that requires minimal pump function in the system due to the large volumetric mass transfer coefficient and resulting small size, the low resistance of the liquid jet and the modular and combined nature of the design. Thus, while embodiments of the present invention achieve unexpected results, an example is a foot that is at least 10 times smaller than a conventional reactor at a capital cost of at least half that of a conventional gas-liquid contactor. Printing and substantially uniform performance are 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 and a gas inlet and outlet. The module further includes a nozzle array in communication with the liquid inlet and the gas inlet, the nozzle array producing a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbance from the gas. The module further includes a gas-liquid separator that allows liquid to pass while at the same time preventing gas from passing. Modules can be connected in series and in parallel with other modules.

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

  The nozzle array can be formed in a plurality of different configurations (eg, a staggered configuration). In a staggered configuration, the first nozzle row, the second nozzle row, and the third nozzle row are offset between the first nozzle row and the third nozzle row by offsetting the second nozzle row. Configured to be located.

  The nozzle array may further include a plurality of nozzles having a predetermined interval. The nozzle may include at least two nozzles separated by a distance greater than about 0.2 cm. The nozzle may include 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 (eg, U-shaped channels, V-shaped channels, etc.) having a plurality of different geometric shapes. Channels can be formed using a variety of methods (including machining or forming a metal, compound, or ceramic plate, or machining the nozzle orifice into a tube or part of a tube). Including, but not limited to). When machining a single plate, a U or U-shaped channel is machined on the liquid side of the plate. The processing sides of these channel plates are 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 processing channel will vary.

  The higher the level of penetration at the intersection, the larger the nozzle is formed. That is, a large nozzle is generated depending on the amount of V or U-shaped channel at the intersection of the cones. When forming a tubular nozzle, the tangential cut point is formed at an angle of approximately 90 degrees with respect to the axis of the radius of the tube (on the processing side) outside the radius. The liquid channel supplying the nozzle has a depth greater than about 2 mm. In embodiments of the present 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 oval shape with a ratio between the major axis and the minor axis of less than 0.5. In other embodiments, the nozzle may have a projected cross-sectional area in the range of about 0.25 mm ² to about 20 mm ² . The projected cross-sectional area is determined by an elevational view of the position of the two-dimensional shape of the nozzle projected onto the two-dimensional surface with the back cooler unit, but the actual shape is both the depth and radius of the cutting point, Of course, and / or it can be three-dimensional and complex based on the shape of the curvature of the channel.

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

In this embodiment, at least a portion of the gas phase molecules is removed by the interrelationship regarding mass transfer between the gas phase molecules and the liquid jet. Vapor phase molecules may include, for example, industrial exhaust from coal-fired power plants, or other industrial exhaust such as pollutants, contaminants (eg, SO _x , NO _x , CO ₂ , Hg) and combinations thereof. Of course, acidic gas such as HCl, HBr, HF, H ₂ SO ₄ , HNO ₃ , CO, H ₂ S, amine (including ammonia), alkanolamine, urea, formamide, alcohol, carboxylate (acetic acid, etc.), Other gas molecules such as combinations thereof and a wide variety of other gas phase molecules can also be removed. The only limitation of the present invention is the ability to provide a range of gas phase molecular reactants or solutes that are reactive or soluble, and a liquid phase. Although the main description of the specification of the present invention is directed to an aqueous solution system, those skilled in the art will readily understand that the invention of the gas-liquid contactor can also be applied to a non-aqueous solution system. For example, partial fluorination of pharmaceuticals or chlorination of petrochemical feedstocks is known.

In one embodiment of the present invention, the liquid may be selected to remove contaminants contained in known gases. The base aqueous solution may be utilized to remove SO _{2 and} other flue gas constituents (eg, solutions containing about 0.1 M to about 1.0 NaOH, NH ₄ HCO ₃ , Na ₂ SO _3, etc.). . As is known, the concentration of these liquid reactants can be adjusted depending on the mass transfer of gas-liquid interactions and the preferred product.

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

Sea water or salt water can be used to clean SO ₂ or CO ₂ , or both, based on pH control or other technical factors. In addition, these liquids are also effective when cleaning other acidic gases such as HCl or HF.

  The method forms at least one jet. 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. Further, the ratio of jet length to width may range from 0.3 to 20.

  As another embodiment of the present invention, a gas-liquid contact system is provided that includes a plurality of combined subsystems. These combined subsystems include a reaction chamber, a gas inlet coupled to the reaction chamber, a gas outlet coupled to the reaction chamber, a liquid plenum coupled to the reaction chamber, a nozzle array coupled to the liquid plenum, and 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 planar liquid sheet, and the plurality of liquid jets are arranged such that they lie in substantially parallel planes.

  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 a high density, high surface area liquid jet (eg, a thin flat liquid jet). 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 processing-side orifice intersects a V-liquid channel having a cone on the opposite side of the groove. However, the resulting nozzle orifice is still elliptical. The orifices included in the nozzle array are staggered such that they are spaced apart from each other. This distance may range 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 need not be constant throughout the orifice array.

  The orifice has a V-shaped inlet 1 and an outlet 2 channel that is conical and leads to the jet. An orifice is formed by the interaction of the 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. A schematic of the jet exiting the orifice is shown in FIG. An enlarged view of the cross section of the inlet 8 and outlet 9 channels is provided. A thin flat liquid jet may be formed with a variable length (eg, the ratio of jet length to jet width is 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 for generating excited oxygen in another embodiment of the present invention. COIL uses a nozzle array in one embodiment of the present invention that has the function of producing a liquid with a large specific area (eg, basic hydrogen peroxide), so it is more efficient and has less weight than prior art designs. Small size. In FIG. 2, COIL is represented by reference numeral 10. The COIL 10 is used when generating excited oxygen. The COIL 10 includes a gaseous reactant source 12 (eg, chlorine gas) attached to a manifold 14. The manifold 14 has a plurality of openings such as holes (not shown) through which a gas jet is inserted into the excited oxygen generation chamber 20. The COIL 10 further has a source of liquid reactant 22 (eg, basic hydrogen peroxide formed with a single base). In one embodiment, the single base is potassium hydroxide (KOH). A source of basic hydrogen peroxide 22 is connected to a plurality of nozzles 26 by pipes 224. The nozzle 26 is configured to form a thin flat jet 28 for liquid basic hydrogen peroxide. The thin flat jet 28 for the hydrogen peroxide 22 reacts with the chlorine gas jet to generate excited oxygen 32. The COIL 10 may further include a method of collecting basic hydrogen peroxide for reuse (eg, a recycle loop).

  By using the liquid jet, the specific surface area of the hydrogen peroxide 22 is increased, and the reaction efficiency with the chlorine gas 12 is increased. Tests have shown that the specific surface area of a thin flat liquid jet is more than three times that of a related art circular jet. In addition to the increased surface area of hydrogen peroxide, flat jets do not require the small throat required by prior art nozzles. More particularly, prior art nozzles had throat sizes ranging from about 150 μm to about 350 μm. Nozzle 26 can utilize a throat greater than about 250 μm, and more preferably a throat greater than 600 μm. Therefore, the nozzle 26 is less likely to be clogged with contaminants (for example, salts generated by the reaction between hydrogen peroxide and chlorine gas). In addition, this allows the system 10 to utilize a basic hydrogen peroxide solution with a high initial molarity (eg, a molarity as high as about 10 moles / L). Prior art systems generally limited the initial molar concentration to 5 mol / L because the system would be clogged with contaminants such as salt. Most systems reuse hydrogen peroxide, but once the molarity drops to about 2.5 mol / L, the system performance degrades significantly. As a result, in most prior art systems, the difference in molar concentration was limited to a range of about 2.5 mol / L to about 5 mol / L, but in this embodiment, the difference in molar concentration is about 2 It can range from 5 mol / L to about 10 mol / L. Thus, the device can carry 1/3 basic hydrogen peroxide of the prior art system and have a capacity three times that of the prior art system.

  In another embodiment, COIL is an excited oxygen generation chamber having a hydrogen peroxide source inlet and a flat jet nozzle for alkaline sources (Li, Na, K) and alkaline earth (Mg, Ca) hypochlorite. including. Hydrogen peroxide is a gas. The nozzle has a plurality of orifices of a minimum size that can generate a thin flat jet having a length exceeding about 300 μm and a large specific surface area. A photon generation chamber is provided having a passage coupled to the excited oxygen generation chamber and an inlet for iodine.

  FIG. 3 is a block diagram of an improved chemical oxygen iodine laser in another embodiment of the present invention. In FIG. 3, the enhanced COIL is indicated generally by the reference numeral 50. The COIL 50 has a source 52 of gas (eg, chlorine gas physically connected to the excited oxygen generation chamber 56 via a plurality of inlets by conduits or pipes 54). A liquid reactant source 58 (eg, basic hydrogen peroxide 58) is transported from the pipe 60 to the flat jet nozzle array 62. The liquid basic hydrogen peroxide 58 is mixed with the chlorine gas 52 by the nozzle 62. By this reaction, excited oxygen 64 containing singlet delta oxygen is generated. Excited oxygen 64 is transported to photon generation chamber 66. An iodine source 68 is coupled to the inlet 70 of the photon generation chamber 66. The iodine source 68 decays the excited oxygen 64 and emits photons. Photon generation chamber 66 has a mirror that provides 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 for regenerating basic hydrogen peroxide for reuse purposes. The COIL 50 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 COIL 50 is more efficient and can be smaller and lighter than prior art systems or can increase laser firing capacity.

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

In this embodiment, the ratio of width to thickness is significantly greater than a factor of 10. For example, at a jet velocity of about 10 m / s, the length of the flat jet stream may be about 15 centimeters or longer. The narrowest passage 100 is where the conical nozzle 90 meets a pair of opposed flat plates 86 and exceeds about 600 μm. The nozzle 80 increases the surface area of the liquid (for example, basic hydrogen peroxide), thereby significantly increasing the reaction efficiency between the basic hydrogen peroxide and chlorine. Furthermore, the large jet surface area and the small jet thickness of the nozzle 80 produce a very large specific surface area ranging from about 10 cm ⁻¹ to about 20 cm ⁻¹ , reducing the generator volume and reducing the laser cavity. The yield of excited oxygen supplied to the is increased. In addition, since the nozzle 80 does not require a small throat or passage that is prone to clogging of contaminants (eg, the salt that results from the reaction of chlorine and basic hydrogen peroxide), the system may have a higher initial molarity. The basic hydrogen peroxide can be used.

  FIG. 5 is a bottom left perspective view 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 ends of a pair of opposed planar plates 86. The only outlet from the second end of the pair of opposed flat plates 86 passes through the conical nozzle. Although the present 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 the gas phase reactant and the liquid phase reactant. As a result, the reaction is significantly more efficient than that of the prior art two-phase reactor design.

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

  <Exhaust contact system and method>

  As described above, System 0 provides a nozzle array that produces a flat jet with a low profile, high density, and high surface area. The system 0 has been described in terms of using COIL. In an alternative embodiment, many of the principles of System 0 are applied to the pollutant mitigation system and method. The contaminant 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.

  Concerning the pollutant mitigation system and method, 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 configuration of the entire pollutant mitigation system and method, In the following, a system implementation example for various pollutants will be described with reference to a schematic diagram with the bottom face up. It will be apparent from the following description that the subcomponents of the pollutant mitigation system and method can be used in numerous applications beyond those relating to the pollutant mitigation system and method.

  <Nozzle>

  As described above, the orifice supplying a flat jet of hydrogen peroxide with respect to system 0 is described. The orifice has a V-shaped inlet 1 and a conical outlet 2 channel for jet forming purposes. The intersection of the inlet 1 and outlet 2 channels forms an orifice. The cross section of the nozzle plate shows the contour of the inlet 3 and outlet 4 channels. A schematic of the jet exiting the orifice is shown in FIG. 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 reactants or sorbents, flat jets do not require the small throat required by related art nozzles. As previously described, related art nozzles have throat sizes in the range of up to about 150 μm to about 350 μm. In contrast, embodiments of the present invention may allow a flat jet nozzle to have a throat about 250 μm or larger compared to the size of a small nozzle. For example, a flat jet nozzle may have a throat in the range of about 250 μm to 2000 μm. Thus, the nozzles of embodiments of the present invention are less likely to become 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 a finer solvent slurry can be utilized. Although high molar concentrations, such as about 10 mol / L, can be utilized, prior art systems typically have an initial molar concentration of about clogging due to clogging of salts and / or solid by-products or precipitates. It was limited to 5 mol / L. Most systems recycle liquid sorbents or reactants, but once the molarity has dropped significantly, the performance of the system is greatly degraded. In embodiments of the present invention, the sorbent or reactant liquid can be easily replenished by simple concentration monitoring and appropriate titration of the reactant into the liquid system.

  The nozzle 1010 shown in FIGS. 8-13 is similar to the conical nozzle 90 described above. For example, similarities can be indicated by the generated nozzle break as an intersection between the approximated cone and the U-shaped channel, although this is not a method that utilizes a cone-shaped machining tool bit. Manufactured. The nozzle 1010 has a configuration that generates a flat jet when the liquid flows and generates a plurality of uniformly spaced flat liquid jets having a shape that can minimize disturbance from the gas in the gas-liquid contact system. A flat jet having plug flow characteristics can also be produced. The initially generated flat jet has very low turbulence characteristics and can maintain the flat jet characteristics for a significant length.

  FIG. 6 is a cross-sectional view of one 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, precursor rods 1012 are utilized to form nozzles 1010 and nozzle banks 1011. The rod 1012 has various dimensions and is generally similar to the flattened shape of the pipe half. The precursor material can take a number of different geometric shapes (eg, oval, oval, semi-circle).

  The rod 1012 has a shell rod thickness 1015, a straight rod height 1016, and a total rod height 1017. In embodiments of the present invention, the shell rod thickness 1015 may range from about 0.015 inches to about 0.055 inches, and the linear height 1016 of the rods from about 0.05 inches to about 0.75. The total rod height 1017 can range from about 0.25 inches to about 0.95 inches. The preferred embodiment shell shell rod thickness 1015 is about 0.035 inches, the maximum measured rod width 1014 is about 0.323 inches, and the linear height 1016 of the rod is about 0.10 inches. Yes, the total height 1017 of the rod may be about 0.31 inches and the rod length 1018 may be about 7.470 inches. The total width 1014 is about 0.323 inches, and the nozzle end 1019 starts at 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. The nozzle bank 1011 is formed using a progressive die. In the first stage of cutting the die, an appropriately sized rectangular metal piece is formed. A single metal or alloy (eg, stainless steel) may be utilized as the die material. In addition, the selection of metals can be made depending on the liquid chemicals utilized and their corrosiveness and reactivity, so other metals including copper, nickel, chromium, aluminum, or alloys containing these metals Can also be selected.

  In the second stage, the specific geometric shapes of FIGS. 6 and 7 are formed. The rod 1012 is preferably 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, nozzle 1010 is formed using an electrical discharge machine (EDM). For example, rod 1012 is attached to a fixture and placed in 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 in the prior art (for example, laser welding). 8 to 13, the 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 the preferred embodiment, the cutting depth 1020 of the nozzle 1010 is about 0.058 inches. The channel depth may range from about 2 mm to 20 mm.

  These nozzles may be formed such that the center 1021 has a uniform distance or a non-uniform distance. In embodiments of the 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, any number of nozzles may be present in the nozzle bank 1011. In the preferred embodiment, the nozzle bank 1011 is formed with 45 nozzles. In addition, end spaces 1022 are formed at both ends of the nozzle bank 1011. In the preferred embodiment, end space 1022 is formed to be approximately 0.235 inches. FIG. 12 shows a state where 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 liquid volume and can provide a large number of jets at low atmospheric contactors at normal atmospheric pressure. In another embodiment, the channel can be machined directly into the plate instead of the welding that has been described. In addition, the nozzle may have a narrow, substantially oval slit (with a minimum dimension of less than about 0.5 mm and a length greater than about 50 mm). Although this nozzle may have an unnecessarily large liquid flow volume compared to the preferred embodiment, it can form a thin flat liquid sheet with a large surface area.

  <Nozzle plate>

  By disposing the nozzle 1010 on the nozzle bank 1011 or the plate 1024, the liquid jet formed by the nozzle is densely filled with a small capacity. By making the fluid flow predictable, the jets are closely packed without interference and without creating turbulence. The fluid flow of the preferred embodiment is such that the incoming liquid flow is about 90 degrees relative to the direction of the liquid nozzle supply channel. It has been found that the best liquid jet properties in water fluids are produced at this time (i.e., for fluid flow along or in parallel with the liquid supply channel, the resulting jet is in a direction along the fluid flow). Changed and adversely affected). In contrast, in a jet laminar flow formed by the nozzle plate 1020, a closely packed jet is generated 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 a 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 numeral 1020. In this embodiment, each of the individual nozzles 1010 is cut into the channel 1015 after being formed, forming a row of nozzles in the channel 1015. Several channels are formed in the plate 1020 to form an orifice plate or nozzle jet array. As described above, the channel 1015 may be a nozzle bank 1011 that is welded to a single plate. Alternatively, the channels and nozzles may be formed from a single plate by machining, and the result is generally as shown in FIGS.

  In the present embodiment, these nozzles 1010 are arranged at an accurate interval to maximize the capacity of the generated jet so that the jet fills the intended volume but does not cross each other. If the distance between the jets is too close, the jets collide with each other or break into small droplets, resulting in an unfavorable result that the effect of the present embodiment is reduced because the flat jet is not in close contact. On the other hand, if the distance between the jets is too large, the specific surface area capable of reacting with gas phase molecules becomes small, and the effect of this embodiment is also reduced. Optimal spacing is determined primarily as a function of 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 and thin flat liquid jets produced by the nozzle plate of FIG. FIG. 19 is a front view of an array of flat and thin flat liquid jets produced by the nozzle plate of FIG. 20 is a side view of an array of flat and thin flat liquid jets produced by the nozzle plate of FIG.

  FIGS. 18-20 show an array or matrix of flat jets that are formed when liquid is forced through the nozzles. 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 have a width of about 2 cm, a length of about 25 cm, and a thickness of about 0.1 mm. Of course, other dimensions can be used. Each nozzle row 1055 forms a row of jets 1060, and a plurality of rows are arranged to form a matrix or array 1065 of flat liquid jets. This plate is configured to form 24 rows of jets 1055. Of course, the number of rows may be adjusted. The number of suitable jet rows may be determined by the size of the gas-liquid contactor and the practical aspects of nozzle array or jet plate manufacture and the associated fluid processing hardware. However, there is no basic restriction on the size on the upper surface side. For very small reactors (for example, those sized for research use), the actual number of rows required to provide two liquid channels is three (and half is the reactor wall) There will be half of one channel on each end). In operation, the gas is configured to flow between the flat jets in parallel to the flat side of the jet, resulting in a very large surface area and intimate contact.

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

  With reference to FIGS. 21 and 22, the nozzle plate is generally designated by reference numeral 1101. The nozzle plate 1101 includes a plurality of nozzles 1010 that are offset and have a staggered configuration. In one embodiment, as shown in FIG. 18, the gas may be configured to flow parallel to the flat surface generated by the jet. The staggered or offset configuration of the nozzle 1010 shields the gas cross-flow channels rather than turbulent flow, so the flow can be increased slightly compared to non-staggered configurations.

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

  Referring to FIGS. 23 and 24, the nozzle plate is generally indicated by reference numeral 1110. The fluid exits 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 includes a plurality of nozzles 1010, which are set in the above-described nozzle array 1112 (see the nozzle bank 1011). 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 when the nozzles are corroded or when the nozzle dimensions need to be changed (eg when using different fluids with different viscosities). become.

  FIG. 25 shows the fluid outlet side of the nozzle plate with the nozzle bank removed. FIG. 26 shows the fluid inlet side of the nozzle plate of FIG. FIGS. 25-26 illustrate the nozzle row 1113 being removable from the nozzle array assembly 1120 and the nozzle bank 1113 being 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 rather than replacing the entire plate. In addition, the removable nozzle bank 1113 helps to adjust the specific area of the contactor and assists in the manufacturing process (eg, gas phase molecules with very high mass transfer can increase trapping or reaction yield). Less specific area to meet). Thus, the nozzle bank can be potentially removed for the purpose of reducing the total liquid flow 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 slightly flattened or formed from a flat sheet on a mandrel. A plurality of nozzles 1010 were cut into tubes 1130. This is an alternative method of nozzle bank formation. The tube 1130 is shown in a flat state and is provided with a groove formed with an electric discharge machine (EDM) for orifice manufacture. When the tube 1130 is cut in the length direction and the non-flat end portion is removed, the groove 1113 is substantially completed and can be fitted into the nozzle plate 1120.

  <Gas-liquid contactor>

  FIG. 29 is a schematic cut-away view of a gas-liquid contactor according to another embodiment of the present invention. A gas-liquid contactor can increase the efficiency of COIL gas-liquid contactors and reduce 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 even in an air stream.

  These nozzles can be made into an array of nozzle plates that form a closely packed, parallel matrix of planar liquid jets. The flat jet array has an aerodynamic shape and can provide stable jet formation at 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 disturbance from the gas. In addition, the nozzle array produces a liquid sheet that is parallel to the airflow to provide a relatively large contact area and low atmospheric pressure drop. The airflow may traverse the liquid jet (crossflow), backflow, or cocurrent.

  The liquid pressure drop required to generate the jet at the nozzle is also low, which reduces the pump cost on both the liquid side and the gas side. There is a hydraulic drop across the orifice (eg nozzle array) that imposes major constraints. For example, the range of hydraulic pressure at which this embodiment functions is between 2 psi and 50 psi, with the best range being between 3 psi and 15 psi. In addition, even flat fluid pressures below 2 psi can still form thin flat jets (depending on the nozzle dimensions), but the liquid velocity is slow and significant deflection occurs in high velocity airflow. Similarly, good thin flat jets can be generated at pressures above 50 psi, but the energy required to provide this water pressure is high, increasing the parasitic energy loss of the system.

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

  Referring to FIG. 29, a gas-liquid contactor is indicated generally by the reference numeral 1600. In this embodiment, a cross flow configuration is utilized, and the gas flows from the left to the right of the contactor 1600. Liquid enters the top 1610 of the contactor 1600 from the inlet plenum 1630 and flows through the nozzle plate 1640 at the top of the contact chamber 1650 with a strong force. A flat liquid jet is formed by these nozzles and flows down in the chamber. The gas flows from left to right in the system of FIG. 29 between parallel jets, where mass transfer occurs and further passes through the low pressure drop demister 1660 to the outlet 1670. The liquid is collected through an anti-splash grid 1680 on the bottom of the contactor, processed as appropriate, and optionally recycled. Anti-splash grid sub-module 1680 is a grid with holes having a shape to receive a flat jet. The anti-splash guard or gas / fluid separator is also configured to substantially minimize back splash of liquid during operation. The holes in the anti-splash grid 1680 are positioned at a slight angle with respect to the outlets 1700 and / or 1690 of the liquid capture outlet plenum 1620 so that fluid can 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).

  The gas-liquid contactor was originally used in a COIL chemical reactor, but is not limited to this application. Gas-liquid contactors can be used in a number of different applications, such as any application where high efficiency, single stage, low cost, and small footprint contact between gas and liquid is preferred. Some examples include heat transfer where gas and liquid are in direct contact, such as gas cooling, mass transfer such as pollutant absorption from flue gas streams, chemical reaction between liquid and gas, such as COIL applications, and Biological reactions such as aerobic digestion can be mentioned. Multi-stage cross-flow contact is accomplished by connecting the contactors in series and pumping liquid from the downstream contactor outlet to the next upstream contactor inlet. Alternatively, two different liquid sorbents or reactants can be independently pumped into a direct-current gas-liquid contactor to cause a two-stage reaction without the disturbance of a single train stream. Gas-liquid contactor embodiments have properties such as very high volume mass transfer coefficient, low pressure drop, low liquid pressure drop, relatively small size, resistance to clogging, low liquid contamination, low capital and operating costs Create a gas-liquid contactor. This is an orifice plate (here, nozzles) with a special array of nozzles that form a matrix of flat, stable, non-misty liquid jets that are closely packed parallel to each other and parallel to the air stream. (Referred to as a board). One embodiment of a single stage gas-liquid contactor is described below. The gas flow rate and the multiple jet lines determine this single stage contact time.

  In the present embodiment, the jet plate is accommodated in the gas-liquid contactor 1600. The gas enters from the left 1672, passes through the flat liquid jet of the contact chamber 1650, passes through the demister 1660, and exits from the gas outlet 1670. Liquid enters from the input plenum 1630, rushes down a series of nozzle plates 1640, forms a flat liquid jet, then passes through a gas-liquid separator 1680 and enters a liquid collection chamber 1620 at the bottom of the contactor. The liquid then exits outlets 1690 and 1700 to be processed and / or recycled.

  FIG. 30 shows a schematic arrangement of a plurality of gas-liquid contactors in another embodiment of the present invention. Referring to FIG. 30, a multi-stage cross-flow device contactor is generally designated by the reference numeral 3000 and is 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 three 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. A continuous contactor may be a concept that is substantially similar to continuous chemical extraction known in the art. The airflow passes through each contactor and the liquid flows as a cross flow from the downstream end 3008 to the upstream end 3010 of the train.

  Liquid is provided to each contactor by a liquid pump (not shown) between each stage. Optionally, a single liquid supply plenum can provide functionality for all gas-liquid contactor modules installed in series, with a single liquid pump delivering that liquid to a single All that is required is to provide a serial liquid supply plenum or supply 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 formed from stainless steel. The material 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 coated with particles, 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 composites thereof.

  <Pollutant removal with ammonia water>

  Embodiments of the invention described herein can be used for applications that remove pollutants from exhaust by utilizing ammonia. An important cost driver for pollutant removal is the low partial pressure of pollutants in the flue gas or low gas absorption. For example, the reaction rate is generally determined as a function of the initial concentration of reactants, with higher concentrations resulting in faster reactions. However, at low initial concentrations, mass transfer becomes a variable that imposes constraints on the reaction or removal of gas or liquid molecules. In an embodiment of the invention, the low mass transfer coefficient is offset with a high relative specific area and high flow rate.

In the related art, a flue gas (FGD) desulfurization system is developed and installed in a power plant to address the problem of SO ₂ and SO ₃ becoming acid rain and air pollution. Most FGD systems absorb SO ₂ as CaSO ₃ by contacting the flue gas with wet limestone, and then oxidize, precipitate, sell, or landfill to CaSO ₄ (Gypsum). The disadvantage of lime or limestone based FD is that they cannot accommodate various pollutants (eg, NO _x , Hg, or CO ₂ ). Another drawback is that the FGD system requires a large footprint and capital investment (such as spray towers and oxidation tanks).

Suitable sorbents for high gas absorption and removal have characteristics such as high liquid jet performance, high gas loading capacity, high oxidative stability, low reaction heat, low sorbent cost, low corrosivity, and marketable product streams. It is a system that has. An example of a sorbent is ammonia water. Ammonia, ammonium salts, and uric acid to inject the boiler or the flue gas, it is possible to reduce the NO _x by selective catalytic reduction (SCR) or selective non-catalytic reduction (SNCR). Ammonia and its salts can control SO _x and multiple contaminants.

By addition related art, a plurality of contaminant control utilizing aqueous absorbing agent is a major component of the NO _x in the combustion exhaust gas NO is by selective catalytic reduction (SCR) or selective non-catalytic reduction (SNCR) N It needs to be reduced to ₂ or oxidized to NO ₂ because NO has very low solubility in water. When oxidized to NO ₂ , NO _x can be absorbed with a basic solution or nitric acid. When using an ammonia-based system, valuable by-products are produced. Ammonium nitrate and ammonium sulfate can be used as fertilizers. Ammonia is effective for capturing CO ₂ than monoethanolamine (MEA) or diethanolamine (DEA), CO ₂ is superior as a recovery means for oilfield.

Embodiments of the present invention capture a number of target pollutants (eg, including but not limited to acid gases, ammonia, VOC, SO _x , NO _x , CO ₂ , Hg, and combinations thereof). be able to. In addition, some embodiments of the invention have a single, small footprint, system and are configured to produce valuable by-products. In addition, since there is no contact with the slurry in the embodiment, processing of the associated material does not become difficult. By not using the slurry, it is not necessary to use the heat to complete the phase change in the ammonia regenerator (or CO ₂ stripper).

In an embodiment of the present invention, the fly ash is removed from the combustion exhaust gas with a bag house or an electrostatic precipitator (ESP), and appropriately cooled for the first wet contact. Then, SO ₂ and NO of the combustion exhaust gas may be oxidized with gaseous hydrogen peroxide, or may be oxidized with a first gas cleaning device using an aqueous hydrogen peroxide solution. The gas scrubber is a horizontal cross-flow gas-liquid contactor that is highly efficient and has a small footprint, as described herein. The gas scrubber cleans the fuel exhaust gas with basic aqueous ammonium sulfate to remove acidic gases (SO ₂ , SO ₃ , NO ₂ , 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. Thereby, the gas is converted into a soluble ammonium salt, and its vapor pressure is reduced to substantially zero. Than about 99% of the absorbance of the SO _x good results. Mercury can also be removed by oxidation and / or absorption processes (HgO _x is much more soluble than elemental Hg). Some reaction mechanisms for contaminant removal in some embodiments of the invention are as follows.
NH ₃ hydrolysis:
_{NH 3 + H 2 O ⇔ NH} 4 + + OH - (1)
SO ₂ capture:
_{H 2 O + SO 2 → H} + + HSO 3 - (2)
^{_{1 / 2O 2 + HSO 3 -}} → HSO 4 - (3)
^{_{2NH 3 + HSO 4 - + H}} 2 O → (NH 4) 2 SO 4 + OH - ( ammonium sulfate) (4)
NO _x capture:
NH ₃ + H ₂ O ⇔ NH ₄ ⁺ + OH- (5)
^{_{H 2 O 2 + OH - →}} HO 2 - + H 2 O (6)
^{_{HO 2 - + NO → NO 2}} + OH - (7)
2NO ₂ + H ₂ O ₂ → 2HNO ₃ (8)
NH ₃ + HNO ₃ → NH ₄ NO ₃ (ammonium nitrate) (9)
Hg capture
H ₂ O ₂ + Hg ⁰ → Hg (II) + product (10)
H ₂ S capture
_{H 2 S (aq) → HS} - + H + (11)
^{_{HS - + NH 3 + H +}} → NH 4 HS (12)

As sulfur and nitric oxide are captured as salts (NH ₄ ) NO ₃ and (NH ₄ ) ₂ SO ₄ , the contact solution concentrates and precipitates and is sold or processed. Heavy metals (Hg) and halides (Cl and F) are precipitated in a separate pH adjustment step. The diluted contact solution is recycled to the gas scrubber.

The flue gas that has undergone these processes is even better than one that has been cleaned with 95% of all pollutants removed and is ready to partially remove CO ₂ . The second gas cleaning device uses a combination of ammonia water and / or ammonia salt as the liquid. CO ₂ is absorbed and reacts with ammonium carbonate and water to form ammonium bicarbonate. For low temperatures and high pH, CO ₂ absorption is preferred. Make-up ammonia controls pH and the level of free ammonia in the gas wash solution. A high ammonia concentration increases the pH, increases CO ₂ absorption and CO ₂ loading, and further increases the vapor pressure of ammonia. A simplified reaction mechanism for CO ₂ capture in embodiments of the present invention includes:
2NH ₃ + H ₂ O + CO ₂ ⇔ (NH ₄ ) ₂ -CO ₃ (Ammonium carbonate) (13)
(NH ₄ ) ₂ CO ₃ + CO ₂ + H ₂ O ⇔ 2NH ₄ HCO ₃ (Ammonium bicarbonate) (14)

A highly concentrated solution from the contactor is sent to a CO ₂ stripper where it is warmed and reverse reaction is performed to release gaseous CO _{2 and} produce ammonium carbonate. The release of CO ₂ is preferred for high temperatures and low pH. Since absorption of ammonia is suitable for low pH, release of CO ₂ is promoted by low pH, and ammonia can remain in the solution. The CO ₂ is separated and compressed to return ammonium carbonate to the gas scrubber.

  A common problem with related art ammonia-based systems 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 creates a visible plume when ammonia reacts with the components of the flue gas to precipitate solids. In addition, ammonia slip significantly increases reagent costs.

In one embodiment, a plurality of gas-liquid contactors shown in FIG. 30 are used for contaminant removal. In this embodiment, each gas-liquid can be configured for different purposes. For example, the gas-liquid contactor 3006 may be specifically designed to capture all ammonia that may slip in the first two contactors 3002, 3004, respectively. In this embodiment, the optimum pH for absorbing acidic gases (SO _x , NO _x , and CO ₂ ) is greater than 7, because the vapor pressure of these gases is lowest at high pH. However, the vapor pressure of ammonia is highest at a high pH. Under optimal conditions of the first gas-liquid contactor 3002, SO ₂ can be captured better than about 99%. The third contactor 3006 can cause the first gas-liquid contactor 3002 and the second gas-liquid contactor 3004 to operate with high ammonia slip under conditions optimal for absorbing acid gas. This is possible because the third contactor 3006 is operated under conditions optimal for capturing ammonia. The captured ammonia is returned to the first two gas-liquid contactors. The fact that the gas-liquid contactor is highly efficient and small means that a third gas-liquid contactor can be provided, which means that a very high capture efficiency is achieved.

  In this embodiment, multiple types of efficiency (from energy consumption and removal system cost reduction, achieving high efficiency of removing multiple pollutants from combustion exhaust gas, minimizing the size of the removal system, from combustion exhaust gas Achieves high efficiency of removing multiple pollutants, and removes multiple pollutants from flue gas by creating a modular system that can be combined in parallel to adapt to various equipment sizes From flue gas by creating a modular system with very low flow resistance (pressure drop) that can be combined in series to achieve high efficiency, selective and continuous removal of pollutants Achieve high efficiency, duplicate (high availability) and maintainability (periodic maintenance) to remove multiple contaminants Achieve high efficiency of removing multiple pollutants from flue gas by creating a modular system that can be combined to provide selective access or for unit failure), mass production in assembly line process Achieve high efficiency of removing multiple pollutants from flue gas by creating possible modular system, and multiple pollutants from flue gas from various types and sizes of power generation and chemical process equipment Achievement of high efficiency).

  Further embodiments are described as a method and system for making a selectively high mass transfer rate of flue gas pollutants from a large volume flue gas flow rate into a continuously replenished liquid constrained to a low system volume. sell. In the present method and system, a dense packed array of high viscosity, wide, thin, long and stable jets react with a high velocity flue gas stream. The orifice forming the jet can be optimized based on the properties of the liquid sorbent such as viscosity and surface tension. Crossflow and backflow designs represent two different embodiments.

The efficiency of the method and system is the modularity of large volumetric mass transfer and resulting compactness, low pressure sorbent processing that requires minimal pump function, and low resistance and design of aerodynamically formed jets And this is achieved by a low pressure flue gas pressure drop throughout the system due to the low resistance due to the combinable nature. See also Table 3-4. Thereby, the efficiency of the process of removing pollutants from the combustion exhaust gas is remarkably increased, and the removal of pollutants such as CO ₂ , SO _x , NO _x , and Hg is economically possible.

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

FIG. 31 is a schematic diagram of a multiple contaminant removal system in one embodiment. In FIG. 31, a multiple contaminant removal system is indicated generally by the reference numeral 2100. System 2100 may be configured to capture SO _x , NO _x , CO ₂ , Hg, HCl, and HF. In the present embodiment, the flue gas 2120 from the boiler 2110 is first washed to remove fine particles such as fly ash at a specific removal point 2130 (for example, a sedimentation chamber or a net filter), and is cooled by a cooling station 2140 as appropriate. . At time 2150, the fuel gas generally includes N ₂ , H ₂ O, CO ₂ , SO ₂ , 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 salt in a highly efficient gas-liquid contactor 2160 as described herein. The dissolved ammonia salt is from the recycle stream 2170 from the float 2110 from the precipitation step 2190 and is ammonium sulfite (SO ₃ ), sulfate (SO ₄ ), nitrate (NO ₃ ), chloride ( Cl), fluoride (F), and optionally a small amount of carbonate (CO ₃ ), and bicarbonate (HCO ₃ ). Ammonium carbonate and ammonium bicarbonate may be kept to a minimum by utilizing a near stoichiometric amount of make-up ammonia.

In step 2165, liquid phase oxidation is performed in the gas-liquid contactor described in the embodiment of the present invention. Of course, several oxidants can be used to convert NO to NO ₂ to obtain better absorbency. SO ₃ ^{− is} also oxidized to liquid phase SO ₄ ²⁻ . Liquid bleed stream 2220 is sent to a precipitator to remove heavy metals and ammonia salts. In the first step 2230, heavy metals (such as Hg) are precipitated 2210 by adjusting the pH. In a second step 2190, the liquid is concentrated to precipitate the ammonia salt. The heavy metal solids from the precipitation step are appropriately processed (2240) and the ammonium salt solids are sold as fertilizer (2250). If the ammonia salt can be sold as concentrated liquid fertilizer after removal of Hg, the second precipitation step can be omitted.

Next, the fuel exhaust gas 2120 containing only N ₂ , H ₂ O, and CO ₂ is converted to ammonia and dissolved ammonium carbonate / bicarbonate in another high efficiency gas-liquid contactor 2260 as described herein. Make contact. Again, ammonia is the make-up stream and the dissolved salt is from recycle stream 2270. Ammonia is added to the object to keep the pH of the contact liquid optimal. CO ₂ is absorbed as ammonium bicarbonate in the liquid sent to the CO ₂ stripper 2280. Here, the temperature is raised (and the pH is adjusted as necessary), the reverse reaction is performed, CO ₂ is released as a gas 2290, and the ammonium carbonate remains in the liquid phase 2300, and the CO ₂ absorber To recycle. The CO ₂ may then be compressed (2310) and sold or sequestered (2320). For the sequestration process, degraded natural gas wells, secondary oil recovery, and other methods can be used, but these are outside the scope of the present invention and will not be described in detail.

After the CO ₂ absorption step, the flue gas is contacted with water in a third high efficiency contactor 2330 as described to strip out any ammonia that may slip from the previous contactor. The pH of the contact liquid (water) is adjusted as necessary to completely absorb ammonia. The bleed stream 2340 may be sent to a CO ₂ stripper 2300 or SO _x absorber.

Finally, the cleaned flue gas 2350 composed of nitrogen, water, some oxygen, and unabsorbed CO ₂ is heated at 2360 to reduce the condensation and send it to the ID fan 2370 and the stack. . By interconnecting the flue gas heater 2360 and the cooler 2140 to a liquid heat carrier, the process can be performed economically. The cooling liquid is brought into contact with the hot flue gas in the gas-liquid heat exchanger 2140. The cooled combustion exhaust gas is sent to the first absorber 2160. The now hot liquid is sent to the downstream flue gas heater 2360 where it is contacted 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 for exhaust to the surroundings. The hot liquid can also be utilized as a heat input to the CO ₂ stripper 2300.

As an option, the waste heat generated in the industrial process can be used as a heat source for CO ₂ strip or exhaust reheating, thereby eliminating the dew protection process. For example, in a power plant this can be obtained from a fly ash bag house.

Optionally, the process can be modified to omit the CO ₂ capture process as appropriate. That is, the system can be focused on SO _x , NO _x , Hg, HCl and HF capture treatments and producing ammonium sulfate and nitrate as fertilizer.

FIG. 32 is a schematic diagram of a multiple contaminant removal system in another embodiment of the present invention. The process of FIG. 32 is simplified to perform only the capture process of SO _x , HCl, and HF only. The process 2400 is designed to capture only the most easily absorbed acid gas. The combustion exhaust gas 2120 from the boiler 2110 is first washed to remove fine particles such as fly ash at a specific removal point 2130 (for example, a precipitation chamber or a net filter), and is cooled by a cooling station 2140 as appropriate. At time 2150, the flue gas generally contains N ₂ , H ₂ O, CO ₂ , SO ₂ , NO, Hg, HCl, and HF.

Thereafter, the flue gas 2150 is contacted with sodium hydroxide or sulfate / sulfite salt from the recycle stream 2420 in a high efficiency gas-liquid contactor 2410 as described herein. Oxidation step 2430 is performed in the liquid phase in the gas-liquid contactor. Oxidation of sulfite (SO ₃ ²⁻ ) using oxygen contained in air or combustion exhaust gas produces liquid phase sulfate (SO ₄ ²⁻ ). Liquid bleed stream 2440 is sent to a precipitator 2450 to remove heavy metals and sulfate salts. In the first step 2460, heavy metals (such as Hg) are precipitated by pH adjustment 2460. In the second step, calcium hydroxide 2470 can be added to precipitate the calcium sulfate, which can be separated, dried, and removed with a precipitator 2480. The float 2490 from the precipitator is returned to the recycle stream. The heavy metal solids produced in the precipitation step may be appropriately processed (2510) and calcium sulfate can be sold as a gypsum (2520).

Finally, the cleaned flue gas 2350 composed of nitrogen, water, NO _x , and CO ₂ is heated by the heater 2360 to reduce the condensed state and sent to the ID fan and stack 2370. As described above, the process can be performed economically by interconnecting the flue gas heater 2360 and cooler 2140 to a liquid heat carrier.

<SO ₂ removal>

SO ₂ in the various performance areas for enhancing the capture function is to reduce the container size and the pressure drop across the reactor, and results in a salable byproduct efficient mass transfer that like to use the saw venting system included. To achieve the performance to be those subject requires innovative design method connects the production stream with value-added high SO ₂ absorption kinetics.

The gas-liquid mass transfer process is performed along the gas-liquid interface. Absorptance of the liquid sorbent of gas, liquid phase mass transfer coefficient k _L, the specific surface area (the ratio of the volume of the surface area of the gas-liquid interface) a, and, between the bulk fluid C _L and the gas-liquid interface C _L ^* Controlled by concentration gradient. In many gas-liquid reaction systems, the solubility of C _L ^* is low 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 present gas-liquid contactor, a method of increasing the ratio of mass transfer kinetics, gas-liquid mixing and / or interfacial surface area to volume is taken.

In an embodiment of the present invention, the cooler Imstone / lime (CaCO ₃ ), sodium carbonate (Na ₂ CO ₃ ) / sodium hydroxide (NaOH), ammonium hydroxide (usually ammonia) that efficiently captures SO ₂ A wide variety of aqueous solutions, including but not limited to water, including water, the abbreviation is AA), double alkali (sodium hydroxide added with lime), magnesium oxide (MgO), zinc oxide (ZnO) A contactor can be utilized with the solvent of. The addition of an oxidant (OX) promotes the oxidation of SO ₂ , thereby promoting the formation of sulfate SO ₄ ²⁻ . In a preferred embodiment, the OX agent is hydrogen peroxide (H ₂ O ₂ ). The combined use of aqueous ammonia and hydrogen peroxide is particularly suitable because it produces a by-product stream that produces a salable profit, such as ammonium sulfate (fertilizer). In addition, H ₂ O ₂ decomposition products (water and oxygen) are environmentally and equipment friendly.

Chemical steps available in SO ₂ oxidation during that contains ammonium hydroxide and hydrogen peroxide aqueous are as follows.
_{NH 3 + H 2 O + SO} 2 → NH 4 + + HSO 3 - (1)
^{_{NH 4 + + HSO 3 - +}} NH 3 → 2NH 4 2+ + SO 3 2- (2)
H ₂ O ₂ + SO ₃ ^2- → H ₂ O + SO ₄ ^2- (3)
2NH ₄ ⁺ + SO ₄ ^2- → NH ₄ SO ₄ (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 having a reshaped orifice plate (or described nozzle plate) and a fluid synthesis technique that is compatible with a wide range of fluids and processing conditions. The removal of SO ₂ is performed by passing gas from a high surface to a volumetric gas-liquid contact unit. Exhaust gas passes through a gas-liquid contactor in a horizontal direction (referred to as crossflow) that has a substantially smaller contactor volume and airflow pressure drop than the related art. A plurality of low-pressure, vertical flat jet arrays having an aqueous sorbent and a substantial surface area run across the crossflow. By adopting an aerodynamic shape, the flat jet array forms a stable jet flow with less liquid particle contamination at a relatively high gas velocity.

In a preferred embodiment, the sorbent for absorption and removal of sulfur dioxide has high SO ₂ capacity, high oxidative stability, low heat of reaction, low saw vent cost, low corrosivity, and salable product stream such characteristics System. An example of an effective SO ₂ removal solvent is an aqueous solution containing 28 wt% ammonia. To optimize the contactor, from a fluid and jet performance standpoint, from about 1% to about 2% polymer or suspension can be added to the aqueous ammonia solution to enhance the contactor performance. Examples of the additive include those that do not react with aqueous ammonia and do not hinder mass transfer. The polymer or suspension allows the formation of sorbent properties (eg, viscosity) that can achieve maximum jet performance (jet width, length, thickness, surface area) with minimal liquid side pressure drop. An example of a polymer additive is diethylene glycol. Examples of other polymer additives include polyethylene oxide or polyvinyl alcohol. An example of an inorganic additive is bentonite.

It is preferable to assist the oxidation rate and thus mass transfer kinetics of SO ₂ to include a further chemical compound. One example of an additive to a suitable sorbent system is hydrogen peroxide. Stabilizers are added to the sorbent mixture to avoid excessive decomposition of hydrogen peroxide at high pH. One example of a stabilizer for hydrogen peroxide at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide can be further improved by adding a hydrogen peroxide catalyst. An example of a hydrogen oxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

  FIG. 33 is a schematic view of a general gas-liquid contactor that generates 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 and supplies gas to the gas-liquid contactor 2645. The system further includes a liquid reagent tank 2610 coupled to a pump 2615 and a liquid capture tank 2620. The capture tank 2620 is connected to the gas / liquid contactor 2645 to collect liquid from the gas / liquid contactor 2645. Optionally, capture tank 2625 may be coupled to liquid recirculation pump 2625. The liquid recirculation pump 2625 can perform a liquid recirculation method. Flow control valve 2630 is coupled to liquid plenum 2635 to control liquid to liquid plenum 2635. A nozzle array 2640 for forming a liquid jet is coupled 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 gas from the liquid sorbent jet is disposed within the gas-liquid contactor 2645. A demister 2660 that can remove small gas droplets from the exiting gas is positioned near the gas outlet 2655.

The gas inlet may contain a plurality of different gases. For example, industrial exhaust such as pollutants, pollutants, etc. that may include SO _x , NO _x , CO ₂ , Hg, and combinations thereof may be included. Of course, HCl, HBr, HF, H ₂ SO ₄ , HNO ₃ , CO, H ₂ S, amine (including ammonia), alkanolamine, urea, formamide, alcohol, carboxylate (such as acetic acid), combinations thereof and Other gas molecules such as acid gases such as a wide variety of other gas phase molecules can also be removed. The only limitation of the present invention is the ability to provide a range of gas phase molecular reactants or solutes that are reactive or soluble, and a liquid phase. Although the main description of the specification of the present invention is directed to an aqueous solution system, those skilled in the art will readily understand that the invention of the gas-liquid contactor can be applied to a non-aqueous system.

In this embodiment, a method for injecting exhaust gas containing SO ₂ into a gas-liquid chamber is described. The gas plenum flows gas evenly throughout the liquid flat jet. The liquid jet is generated by pumping the sorbent into the liquid plenum and spreading the sorbent across the nozzle orifice. The generated jet flows down vertically into the contact chamber, passes through the gas-liquid separator and reaches the capture tank. In the gas-liquid chamber, a vertically flowing sorbent intersects the gas cross-flow. Sulfur dioxide is absorbed by the sorbent liquid and removed from the exhaust gas stream. The exhaust gas after cleaning is discharged from the outlet of the contact chamber. The sorbent is recirculated to continuously remove SO ₂ from the exhaust gas stream.

The performance of the gas liquid contactor is shown on the small subscale test bed of FIG. Table 4 summarizes the geometric parameters in this example.

  The jet orifice configuration utilized 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 optimization with respect to jet surface area (length and width) is possible by using additives (eg diethylene glycol) to improve sorbent viscosity / surface tension properties or by reshaping the orifice nozzle.

An example of operating conditions and performance of the gas-liquid contactor is shown in Table 5. A sorbent system containing about 28% by weight aqueous ammonia was tested. No additive involved in viscosity or oxidation is added to the sorbent mixture. As the exhaust gas, N ₂ with 500 ppmv of SO ₂ was used. The gas mixture was injected into the contactor under atmospheric temperature and atmospheric pressure conditions and measured using a calibrated mass flow controller. The volume flow rate of the liquid was measured by recording the amount discharged into the container on the receiver side where the liquid jet was calibrated at the measured time interval. The test result for SO ₂ absorption under the above test conditions was that 95% of SO ₂ was removed without the use of an oxidizer accelerator (H ₂ O ₂ ).

<NO _x capture device>

Another embodiment of the invention relates to NO _x capture by use of a gas-liquid contactor. NO _x is a major pollutant consisting mainly of nitric oxide (NO) and nitrogen dioxide (NO ₂ ). Depending on the combustion process, account for greater than 90 percent of the NO _x is nitric oxide. NO _x is produced by the reaction of nitrogen and oxygen at high combustion temperatures (> 2700 degrees Fahrenheit) and by the oxidation of nitrogen in the fuel. Various performance areas for improving NO ₂ capture capabilities include reducing reactor vessel size and pressure drop, utilizing an efficient mass transfer sorbent system, and the like.

The gas-liquid mass transfer process is performed at the gas-liquid interface. Absorptance of the liquid sorbent of gas, liquid phase mass transfer coefficient k _L, the specific surface area (the ratio of the volume of the surface area of the gas-liquid interface) a, and, between the bulk fluid C _L and the gas-liquid interface C _L ^* Controlled by concentration gradient. In many gas-liquid reaction systems, the solubility of C _L ^* is low and there is a limit to the control of the concentration gradient. In order to increase the gas absorption rate, the present gas-liquid contactor needs to be designed to increase the mass transfer kinetics, gas-liquid mixing and the ratio of interfacial surface area to volume.

One embodiment of the present invention includes a high performance gas-liquid contactor such as described with reference to FIG. The system can improve overall mass transfer and contactor performance by utilizing a high density, high surface area, thin aerodynamic shaped flat jet. The gas-liquid contactor has an improved specific surface area of about 1 cm ⁻² to about 50 cm ⁻² , a generator volume of about 1/10 of the volume of a related art packed tower, and a contactor pressure drop of 5 torr / linear ft ( low, such as less than lineal ft), liquid jet drive pressure is less than 50 psi (more preferably less than 20 psi), and liquid entrainment in the gas stream is minimized. It is characterized by that.

In a preferred embodiment, the system has a specific surface area in the range of about 10 cm ⁻¹ to about 20 cm ⁻¹ , a generator volume of about 1/10 of the related art packed column volume, and a contactor pressure drop of 1 Torr / Including features such as less than a linear foot, jet drive pressures in the range of about 5-10 psi, and minimal contamination of liquids into the gas stream.

In order to capture the NO _x efficiently, ammonium hydroxide (usually referred to as aqueous ammonia, an ellipsis is AA), including metal chelates or uric acid gas with sorbent a wide variety of aqueous but not limited to: A liquid contactor can be utilized. Oxidation of NO to NO ₂ is promoted by adding an oxidizing agent (OX), thereby the solvent absorptivity is increased. The various oxidizing agents (OX), sodium chlorite (NaClO _2), sodium (NaOCl) sodium hydroxide hypochlorite - potassium permanganate (KOH-KMnO _4), and hydrogen peroxide _{(H 2} O ₂ ). In a preferred embodiment, the contactor utilizes aqueous ammonia and hydrogen peroxide because the decomposition products of H ₂ O ₂ (water and oxygen) are environmentally and equipment friendly, both of which are conventional in structure. It produces ammonium sulfate that does not spoil the material and can be sold as a crop fertilizer, leading to reduced processing costs.

The oxidation chemistry mechanism of NO and NO ₂ when ammonium hydroxide and hydrogen peroxide are included is believed to be the following.
_{NH 3 + H 2 O → NH} 4 + + OH - (1)
^{_{H 2 O 2 + OH - →}} HO 2 - + H 2 O - (2)
_{HO 2 + NO → NO 2 +} OH - (3)
NO ₂ + NO ₂ → N ₂ O ₄ (4)
N ₂ O ₄ + H ₂ O → HNO ₂ + HNO ₃ (5)
HNO ₂ + H ₂ O ₂ → HNO ₃ + H ₂ O (6)
HNO _{3 ^{(aqueous) → H + + NO 3 -}} (7)
^{_{NH 4 + + NO 3 - →}} NH 4 NO 3 ( nitrate) (8)

One embodiment utilizes an exhaust gas cleaning process that removes sulfur dioxide with high efficiency. The system includes a nozzle array. The nozzle array has a reshaped orifice plate (or nozzle plate) and includes fluid synthesis techniques that are compatible with a wide range of fluids and processing conditions. In this embodiment, NO _x removal is performed by passing gas from a high surface to a volumetric gas-liquid contactor unit. The exhaust gas passes through a gas-liquid contactor having a substantially small contactor volume and airflow pressure drop in the horizontal direction (referred to as crossflow). A plurality of low-pressure, vertical flat jet arrays having an aqueous sorbent and a substantial surface area run across the crossflow. The nozzle array is configured to generate an aerodynamic shape to produce a flat jet array that forms a stable jet stream with less liquid particle contamination at a relatively high gas velocity.

In an embodiment of the present invention, the sorbent for absorption and removal of sulfur dioxide have high NO _X capacity, high oxidative stability, low heat of reaction, low solvent cost, low corrosivity, and salable product stream such characteristics A system can be included. In a preferred embodiment, an example of an effective NO ₂ removal solvent is an aqueous solution containing 28 wt% ammonia. From a fluid and jet performance standpoint, optimize the nozzle plate (described herein) by adding about 1% to about 2% polymer or suspension to the aqueous ammonia solution to enhance contactor performance. Can do. A suitable additive is one that does not react with ammonia water and does not hinder mass transfer. Polymers or suspensions can be utilized that allow the formation of sorbent properties (eg, viscosity) that can achieve maximum jet performance (jet width, length, surface area) with minimum liquid pressure drop. An example of a polymer additive is diethylene glycol. Examples of other polymer additives include polyethylene oxide or polyvinyl alcohol. An example of an inorganic additive is bentonite. Inclusion of additional chemical compounds is preferred to aid in the rate of NO oxidation and thus mass transfer kinetics. One example of an additive to a suitable sorbent system is hydrogen peroxide. Stabilizers are added to the sorbent mixture to avoid excessive decomposition of hydrogen peroxide at high pH. One example of a stabilizer for hydrogen peroxide at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide is further enhanced by adding a hydrogen peroxide catalyst. An example of a hydrogen peroxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

As described with reference to FIG. 33, the present system can be used for NO _x capture. The process is described from injecting exhaust gas containing NO _x into the gas-liquid chamber 2645. The gas plenum 2605 allows gas to flow evenly throughout the liquid flat jet. The liquid jet is generated by pumping the sorbent to the liquid plenum 2635 and spreading the sorbent across the nozzle orifice. The generated jet flows down vertically into the contact chamber and through the gas-liquid separator reaches the capture tank 2620. In the gas-liquid chamber 2645, the vertically flowing sorbent intersects the gas crossflow. Sulfur dioxide is absorbed by the sorbent liquid and removed from the exhaust gas stream. The cleaned exhaust gas 2655 is discharged from the outlet of the contact chamber. The solvent is recycled to continuously remove NO _x from the flue gas stream. The performance of the gas liquid contactor is shown on the small subscale test bed of FIG. Table 6 summarizes the geometric parameters in this example.

  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 with respect to jet surface area (length and width) is possible by using additives (eg, diethylene glycol) to improve the viscosity / surface tension properties of the sorbent or by reshaping the orifice nozzle.

Table 7 shows an example of operating conditions and performance of the gas-liquid contactor. A solvent system containing about 28% by weight aqueous ammonia was tested under any of the operating conditions shown in Table 2. As the solvent, an oxidizing agent (Ox) that promotes removal of NO ₂ or a solvent that does not contain an additive related to viscosity was used. Exhaust gas, using the plus 500ppmv the NO ₂ to nitrogen (N2). The gas mixture was injected into the contactor under atmospheric temperature and atmospheric pressure conditions and measured using a calibrated mass flow controller. The volume flow rate of the liquid was measured by recording the amount discharged into the container on the receiver side where the liquid jet was calibrated at the measured time interval. The concentration of reduced NO ₂ from the contactor can be measured by measuring the light absorption of NO ₂ at 400 nm. The background NO ₂ concentration was recorded before each run. A stable stream of NO ₂ / N ₂ was first generated and the absorbance was recorded without jet flow (A _Off ). A jet stream (28 wt% AA) was then injected into the reactor chamber and the absorbance was recorded. The amount of NO ₂ reduced (the amount absorbed) is expressed as a percentage as follows:% NO ₂ reduction = 100 × (A _off −A _on ) / A _off (1).

FIG. 34 is a graph showing the relationship between absorbency and runtime of the NO ₂ removal system. In FIG. 34, a typical NO ₂ absorption spectrum by on and off of the liquid ammonia water jet is shown. The y-axis represents absorbance at 400 nm and the x-axis represents time in seconds. As can be seen from this example, the short extinction lifetime immediately after the start of the jet flow is due to flow perturbations in the chamber. An average of four test runs was run for each test result. The test results of NO ₂ absorption under the described test conditions were appropriate even if NO ₂ removal was -35% and no oxidation promoter (H ₂ O ₂ ) was present.

  <Hg capture device>

Another embodiment of the invention relates to NO _x capture by use of a gas-liquid contactor. The gas-liquid mass transfer process is performed along the gas-liquid interface. Absorptance of the liquid sorbent of gas, liquid phase mass transfer coefficient k _L, the specific surface area (the ratio of the volume of the surface area of the gas-liquid interface) a, and, between the bulk fluid C _L and the gas-liquid interface C _L ^* Controlled by concentration gradient. In many gas-liquid reaction systems, the graph is very insoluble in C _L ^* and has limited control over the concentration gradient. Therefore, to increase the gas absorption rate, it is necessary to increase the mass transfer dynamics and increase the ratio of the interfacial surface area to the volume.

One embodiment of the present invention includes a high performance gas-liquid contactor such as described with reference to FIG. The system can improve overall mass transfer and contactor performance by utilizing a high density, high surface area, thin aerodynamic shaped flat jet. The gas-liquid contactor has an improved specific surface area of about 1 cm ⁻² to about 50 cm ⁻² , a generator volume of about 1/10 of the related art packed column volume, and a pressure drop across the contactor of 5 torr / linear ft. Low, such as less than (lineal ft), the liquid jet drive pressure is less than 50 psi (more preferably less than 20 psi), and liquid contamination in the gas stream is minimized. Characterized by being.

In a preferred embodiment, the system has a specific surface area in the range of about 10 cm ⁻¹ to about 20 cm ⁻¹ , a generator volume of about 1/10 of the related art packed column volume, and a pressure drop of less than 1 Torr. Including a feature that the jet drive pressure is about 5 psi and that liquid contamination in the gas stream is minimized.

Gas-liquid contactors can be used with various aqueous sorbents that oxidize elemental mercury (Hg ⁰ ) to Hg (II). When in the Hg (II) state, mercury becomes soluble in an aqueous solution, and Hg (II) can remove elemental mercury (HgO) from the exhaust gas stream by catalytic activity. Oxidizing agents (OX) include, but are not limited to, sodium hypochlorite (NaOCl) and hydrogen peroxide (H ₂ O ₂ ). A suitable oxidant for use in the contactor is hydrogen peroxide (H ₂ O ₂ ), with a catalyst (Cat) improving the Hg ⁰ oxidation rate added as an additive. The additive is, 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 the following.
H ₂ O ₂ + Hg ⁰ → Hg (II) + product (1)
H ₂ O ₂ + Cat + Hg ⁰ → Hg (II) + product (2)

  In this embodiment, a highly efficient gas-liquid contactor is used for the exhaust gas cleaning process for removing mercury with high efficiency. The system includes a nozzle array that includes a reshaping orifice plate (or nozzle plate) and includes fluid synthesis techniques that are compatible with a wide range of fluids and processing conditions. Hg removal is accomplished by passing gas from a high surface to a volumetric gas-liquid contactor unit as described in US Pat. No. 7,379,487, incorporated herein by reference. The exhaust gas passes through a gas-liquid contactor having a substantially small contactor volume and airflow pressure drop in the horizontal direction (referred to as crossflow). A plurality of low-pressure, vertical flat jet arrays having an aqueous sorbent and a substantial surface area run across the crossflow. By adopting an aerodynamic shape, the flat jet array forms a stable jet flow with less liquid particle contamination at a relatively high gas velocity.

In a preferred embodiment, mercury absorption and removal is performed by a system having characteristics such as high Hg capacity, high oxidative stability, low heat of reaction, low sorbent cost, low corrosivity, and a product stream that can be sold. An example of a sorbent is an aqueous solution containing about 10 wt% hydrogen peroxide and about 0.1 wt% catalyst to promote the oxidation of element Hg ⁰ to Hg (II). The nozzle plate configuration may be optimized by adding about 1% to about 2% suspension to an aqueous solution of hydrogen peroxide to enhance contactor performance. Additives may be designed so that they do not react with aqueous hydrogen peroxide and do not interfere with mass transfer. Additives allow the formation of sorbent properties (eg, viscosity) that can achieve maximum jet performance (jet width, length, surface area) with minimum liquid pressure drop. An example of an additive is bentonite.

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

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

<H ₂ S capture device>

Another embodiment of the invention relates to the capture of H ₂ S by use of a gas-liquid contactor. Hydrogen sulfide is a highly toxic, flammable and unpleasant odor gas, and is considered a poison in a wide range, but it affects the central nervous system. Artificial hydrogen sulfide sources are mainly generated by processing crude oils with high natural gas and sulfur capacities. The concentration of H ₂ S in natural gas can be up to 28%. Artificial emissions account for about 10% of global H ₂ S emissions. Refinery hydrodesulfurization accounts for the majority of industrial emissions of H ₂ S. Other industrial emission sources for H ₂ S are coke ovens, paper mills, and leather industry.

Environmental issues related to fuel products (gasoline and diesel) with high H ₂ S emissions and high sulfur capacities have led to strict government controls. These regulations have resulted in significant increases in natural gas and oil processing costs. A number of techniques for removing H ₂ S have been proposed so far.

The most prevalent method is the Claus process known in the art, which converts H ₂ S to elemental sulfur by oxyfuel combustion. One problem with the Claus process is that the raw material CO ₂ reacts with H ₂ S to form carbonyl sulfide and carbon disulfide. Another problem is that the unreacted H ₂ S is mixed into the elemental sulfur product as a balance point problem. Other methods of removing H ₂ S include alkanolamines (monoethanolamine, diethanolamine, and methyldiethanolamine), iron oxide / sodium carbonate, thiosarsenate, quinine, and metal vanadium processes. However, there is still no high-performance and cost-effective commercially feasible method for removing H ₂ S from flue gas. Strong cost drivers for H ₂ S capture (except for labor costs and building equipment) are reagent costs, treatment and waste disposal, hardware (absorption containers, flue gas treatment and plumbing) and installation space constraints. is there.

Providing an efficient and cost-effective hydrogen sulfide removal function is a major technical challenge. Various performance areas for improving H ₂ S capture capabilities include reducing reactor vessel size and pressure drop, and utilizing efficient mass transfer solvent systems that produce marketable by-products, etc. included. One embodiment of the present invention relates to achieving these targeted performances with an innovative design approach that links high H ₂ S absorption kinetics with value-added production streams.

  <Flat jet spray contactor>

The gas-liquid mass transfer process is performed along the gas-liquid interface. Absorptance of the liquid sorbent of gas, liquid phase mass transfer coefficient k _L, the specific surface area (the ratio of the volume of the surface area of the gas-liquid interface) a, and, between the bulk fluid C _L and the gas-liquid interface C _L ^* Controlled by concentration gradient. In many gas-liquid reaction systems, the solubility of C _L ^* is low and there is a limit to the control of the concentration gradient. Therefore, to increase the gas absorption rate, it is necessary to increase the mass transfer dynamics and increase the ratio of the interfacial surface area to the volume.

One embodiment of the present invention includes a high performance gas-liquid contactor such as described with reference to FIG. The system can improve overall mass transfer and contactor performance by utilizing a high density, high surface area, thin aerodynamic shaped flat jet. The gas-liquid contactor has an improved specific surface area of about 1 cm ⁻² to about 50 cm ⁻² , a generator volume of about 1/10 of the related art packed column volume, and a pressure drop across the contactor of 5 torr / linear ft. Low, such as less than (lineal ft), the liquid jet drive pressure is less than 50 psi (more preferably less than 20 psi), and liquid contamination in the gas stream is minimized. Characterized by being.

In a preferred embodiment, the system has a specific surface area in the range of about 10 cm ⁻¹ to about 20 cm ⁻¹ , a generator volume of about 1/10 of the related art packed column volume, an atmospheric pressure drop of less than 1 Torr, etc. Features include low, jet drive pressure of about 5 psi, and minimal liquid entrainment in the gas stream.

Gas-liquid contactors can be used with a variety of conventional liquid (aqueous based) solvents that oxidize H ₂ S and other sulfur-based compounds. Oxidizing agents (OX) include aqueous ammonia, alkanolamines (monoethanolamine, diethanolamine, and methyldiethanolamine), iron oxide / sodium carbonate, thiosarsenate, quinine, and metal vanadium processes, sodium hypochlorite (NaOCl), and hydrogen peroxide (H ₂ O ₂ ), but are not limited to these. Suitable oxidants for use in the contactor are basic (pH>) with a catalyst (Cat) added as an additive to improve the oxidation rate and a stabilizer to control the decomposition of hydrogen peroxide. 7) Hydrogen peroxide (H ₂ O ₂ ) aqueous solution. An example of a catalyst additive is TAML (iron (III) tetra-amide macrocyclic ligand). The stabilizer may be, for example, poly-α-hydroxylacrylic acid, sodium silicate, or dimethylenetriaminepentaacetic acid.

It is believed that the chemical mechanism of H ₂ S oxidation that can occur when aqueous basic hydrogen peroxide is included is as follows.
^{_{H 2 S + OH - → HS}} - + H 2 O (1)
^{_{4H 2 O 2 + HS - →}} SO 4 2- + H + + 4H 2 O (2)

<H ₂ S removal process>

The present embodiment relates to an exhaust gas cleaning process for removing hydrogen sulfide with high efficiency. The present invention includes a nozzle array having a reshaped orifice plate (or a nozzle plate as described) and fluid synthesis techniques that are compatible with a wide range of fluids and processing conditions. Removal of H ₂ S is performed by passing gas from a high surface to the volumetric gas-liquid contactor unit. Exhaust gas passes through a gas-liquid contactor in a horizontal direction (referred to as crossflow) that has a substantially smaller contactor volume and airflow pressure drop than the related art. A plurality of low-pressure, vertical flat jet arrays having an aqueous sorbent and a substantial surface area run across the crossflow.

By adopting an aerodynamic shape, the flat jet array forms a stable jet flow with less liquid particle contamination at a relatively high gas velocity. The sorbent for absorption and removal of sulfur dioxide has the characteristics of high H ₂ S capacity, high oxidative stability, low heat of reaction, low solvent cost, low corrosivity, and marketable product stream. An example of a sorbent is an aqueous solution containing about 10 wt% hydrogen peroxide and about 0.1 wt% catalyst to promote H ₂ S oxidation. To optimize the contactor, about 1% to about 2% suspension can be added to the aqueous hydrogen peroxide solution to enhance the contactor performance. Examples of the additive include those that do not react with the aqueous hydrogen peroxide solution and do not hinder mass transfer. Additive examples allow the formation of sorbent properties (eg, viscosity) that can achieve maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. An example of an additive is bentonite.

Inclusion of additional chemical compounds is preferred to aid in the rate of H ₂ S oxidation and thus mass transfer kinetics. One example of an additive to a suitable sorbent system is hydrogen peroxide. Stabilizers are added to the sorbent mixture to avoid excessive decomposition of hydrogen peroxide at high pH. One example of a stabilizer for hydrogen peroxide at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide can be further improved by adding a hydrogen peroxide catalyst. An example of a hydrogen oxide catalyst is iron (III) tetra-amide macrocyclic ligand (TAML).

As described with reference to FIG. 33, the present system can be used for H ₂ S removal. The process is described from injecting an exhaust gas containing H ₂ S into the gas-liquid chamber 2645. The gas plenum 2605 allows gas to flow evenly throughout the liquid flat jet. The liquid jet is generated by pumping the sorbent to the liquid plenum 2635 and spreading the sorbent across the nozzle orifice. The generated jet flows down vertically into the contact chamber and through the gas-liquid separator reaches the capture tank 2620. In the gas-liquid chamber 2645, the vertically flowing solvent intersects the gas cross-flow. Hydrogen sulfide is absorbed by the sorbent liquid and removed from the exhaust gas stream. The cleaned flue gas 2655 is discharged from the outlet of the contact chamber. The sorbent is recirculated to continuously remove H ₂ S from the flue gas stream.

<Flat jet spray contactor of CO ₂ capture device>

Another embodiment relates to CO ₂ capture by use of a gas-liquid contactor. The gas / liquid mass transfer process is performed along the sea surface of the gas / liquid. Absorptance of the liquid solvent gas, the liquid phase mass transfer coefficient k _L, the specific surface area (the ratio of the volume of the surface area of the gas-liquid interface) a, and, between the bulk fluid C _L and the gas-liquid interface C _L ^* Controlled by concentration gradient. In many gas-liquid reaction systems, the solubility of C _L ^* is low and there is a limit to the control of the concentration gradient. In order to increase the gas absorption rate, the present gas-liquid contactor needs to be designed to increase the mass transfer kinetics, gas-liquid mixing and the ratio of interfacial surface area to volume.

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

One embodiment of the present invention includes a high performance gas-liquid contactor such as described with reference to FIG. The system is based on an array that can improve overall mass transfer and contactor performance by utilizing a thin flat jet of high density, high surface area, and aerodynamic shape. The gas-liquid contactor has an improved specific surface area of about 1 cm ⁻² to about 50 cm ⁻² , a generator volume of about 1/10 of the related art packed column volume, and a pressure drop across the contactor of 5 torr / linear ft. Low, such as less than (lineal ft), the liquid jet drive pressure is less than 50 psi (more preferably less than 20 psi), and liquid contamination in the gas stream is minimized. Characterized by being.

In a preferred embodiment, the system has a specific surface area in the range of about 10 cm ⁻¹ to about 20 cm ⁻¹ , a generator volume of about 1/10 of the related art packed column volume, an atmospheric pressure drop of less than 1 Torr, etc. Features include low, liquid jet drive pressure of about 5 psi, and minimal liquid entrainment in the gas stream.

In order to efficiently capture CO ₂ , the contactor is composed of hindered amines such as monoethanolamine (MEA), methylaminopropanol (AMP) and piperazine (PZ), potassium carbonate (K ₂ CO ₃ ) and ammonium hydroxide (usually Can be used with a wide variety of aqueous-based sorbents including, but not limited to, ammonia water (abbreviated AA). The use of a contactor together with aqueous ammonia is particularly suitable because ammonium bicarbonate can be produced and converted into uric acid, which is a fertilizer, or sold as a chemical raw material, and the processing cost is reduced. The chemical mechanism of CO ₂ capture and by-product production in aqueous ammonia is believed to be the following.
2NH ₃ + H ₂ O + CO ₂ → (NH ₄ ) ₂ CO ₃ (ammonium carbonate) (1)
(NH ₄ ) ₂ CO ₃ + CO ₂ + H ₂ O → 2NH ₄ HCO ₃ (ammonium bicarbonate) (2)
NH ₄ HCO ₃ + heat, pressure → (NH ₂ ) ₂ CO (uric acid) (3)

<CO ₂ removal process>

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 includes a nozzle array that includes a reshaping orifice plate (or nozzle plate) and includes fluid synthesis techniques that are compatible with a wide range of fluids and processing conditions. As described above, CO ₂ is removed by passing gas from a large surface to the gas-liquid contact unit. The exhaust gas passes through a gas-liquid contactor having a substantially small contactor volume and airflow pressure drop in the horizontal direction (referred to as crossflow). A plurality of low pressure, vertical flat jet arrays having aqueous solvent and substantial surface area are running across the crossflow. By adopting an aerodynamic shape, the flat jet array forms a stable jet flow with less liquid particle contamination at a relatively high gas velocity. Carbon dioxide absorption and removal sorbents may have properties such as high carbon dioxide capacity, high oxidative stability, low heat of reaction, low solvent cost, low corrosivity, and marketable product streams. An example of an effective CO ₂ removal solvent is an aqueous solution containing 28 wt% 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 the additive include those that do not react with aqueous ammonia and do not hinder mass transfer. Suitable polymers or suspensions allow the formation of sorbent properties (eg, viscosity) that can achieve maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. An example of a polymer additive is diethylene glycol. Examples of other polymer additives include polyethylene oxide or polyvinyl alcohol. An example of an inorganic additive is bentonite.

As described with reference to FIG. 33, the present system can be used for CO ₂ removal. The process is described from injecting exhaust gas containing CO ₂ into the gas-liquid chamber 2645. The gas plenum 2605 allows gas to flow evenly throughout the liquid flat jet. The liquid jet is generated by pumping the sorbent to the liquid plenum 2635 and spreading the sorbent across the nozzle orifice. The generated jet flows down vertically into the contact chamber and through the gas-liquid separator reaches the capture tank 2620. In the gas-liquid chamber 2645, the vertically flowing sorbent intersects the gas crossflow. Carbon dioxide is absorbed by the sorbent liquid and removed from the exhaust gas stream. The cleaned exhaust gas 2655 is discharged from the outlet of the contact chamber. The sorbent is recirculated to continuously remove CO ₂ from the flue gas stream.

The performance of the gas liquid contactor is shown on the small subscale test bed of FIG. Table 7 summarizes the geometric parameters in this example.

  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 with respect to jet surface area (length and width) is possible by using additives (eg diethylene glycol or bentonite) to improve solvent viscosity / surface tension properties or by reshaping the orifice nozzle.

Table 8 shows an example of operating conditions and performance of the gas-liquid contactor. Two sorbent systems, ammonia water and MEA, were tested under any operating condition. No additive related to viscosity is added to the sorbent mixture. The exhaust gas is a mixture of air and CO ₂ , usually mixed with a CO ₂ to air dilution ratio of 1: 9, and injected into a contactor under conditions of atmospheric temperature and atmospheric pressure. Measured using a calibrated mass flow controller. The volume flow rate of the liquid was measured by recording the amount discharged into the container on the receiver side where the liquid jet was calibrated at the measured time interval. The amount of the reduced (absorbed) CO ₂ is the percentage,% CO ₂ reduction _{= 100x (C in -C out)} / C in ... so expressed as (1), _{where, C in} and C _out is the concentration of CO ₂ entering and exiting the contactor. The relative amount of CO ₂ entering and exiting the contactor is determined by integrating the fundamental absorption band of CO ₂ near 4.2 μm with a Fourier transform infrared spectrophotometer (FTIR).

FIG. 35 is a graph of the FTIR (Fourier transform spectrophotometer) absorption spectrum of CO _{2 in which} the liquid ammonia water jet is turned on and off. In FIG. 35, an average of four test runs was run for each test result. The background CO ₂ concentration was recorded before each run. The test results for CO ₂ absorption under the described test conditions were such that CO ₂ removal exceeded 90%. Graph, the absorbance of CO ₂ molecules, was the light range of the fundamental absorption region of 2250 cm ^-1 from 2400 cm ^-1. The graph clearly shows the reduction of light absorbing species in the basic CO ₂ region, indicating that efficient removal has occurred. By performing a basic mathematical analysis on these spectra, the concentration giving these absorbance levels is known, and by examining these proportions, removal can be expressed as a percentage.

  <Flat jet spray contactor system for removing gaseous pollutants>

  In embodiments of the present invention, gas stream contaminants can be removed by a gas-liquid contactor. 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 contaminants dissolve in the sorbent, they are dissolved or absorbed into the liquid sorbent and removed from the gas stream. The extent of the absorption process is governed by mass transfer processes, which include gas and liquid diffusion, and solubility and chemical reactions.

The gas-liquid mass transfer process is performed along the gas-liquid interface. Absorptance of the liquid solvent gas, the liquid phase mass transfer coefficient k _L, the specific surface area (the ratio of the volume of the surface area of the gas-liquid interface) a, and, between the bulk fluid C _L and the gas-liquid interface C _L ^* Controlled by concentration gradient. In many gas-liquid reaction systems, control of the concentration gradient is limited due to the low solubility of C _L ^* . In order to increase the gas absorption rate, the present gas-liquid contactor needs to be designed to increase the mass transfer kinetics, gas-liquid mixing and the ratio of interfacial surface area to volume.

One embodiment of the invention includes a high performance gas liquid contactor as described herein. The system can improve overall mass transfer and contactor performance by utilizing a high density, high surface area, thin aerodynamic shaped flat jet. The gas-liquid contactor has an improved specific surface area of about 1 cm ⁻² to about 50 cm ⁻² , a generator volume of about 1/10 of the related art packed column volume, and a pressure drop across the contactor of 5 torr / linear ft. Low, such as less than (lineal ft), the liquid jet drive pressure is less than 50 psi (more preferably less than 20 psi), and liquid contamination in the gas stream is minimized. Characterized by being.

In a preferred embodiment, the system has a specific surface area in the range of about 10 cm ⁻¹ to about 20 cm ⁻¹ , a generator volume of about 1/10 of the related art packed column volume, and a pressure drop of less than 1 Torr. Including a feature that the jet drive pressure is about 5 psi and that liquid contamination in the gas stream is minimized.

Various types of aqueous sorbents are used in combination with polymer additives to capture efficient gaseous contaminants and improve jet surface area. Acidic gases such as H ₂ S and CO ₂ are usually removed with alkanolamines, monoethanolamine (MEA) and diethanolamine (DEA). SO ₂ and NOx sorbent basic includes calcium carbonate mixture (Limestone / Lime) and ammonium hydroxide (aqueous ammonia), respectively. A sorbent system with a customized sorbent system is preferred because the contamination control contactor can be simplified and miniaturized. An all-in-one system can be configured in series or in parallel. In addition, an all-in-one system utilizes the gas-liquid contactor described herein.

In preferred embodiments, the additive that improves jet surface area is polyvinyl alcohol, polyvinyl oxide, ethylene glycol or diethylene glycol. Inorganic suspensions (eg, bentonite) are also suitable for the treatment to improve the jet surface area. Ammonia water is a suitable sorbent because it has a function of removing CO ₂ , SO ₂ , NO _x and H ₂ S. By adding an oxidizing agent (for example, hydrogen peroxide), it is possible to help the oxidation of NO and Hg which are not easily absorbed by the aqueous solution. Catalysts that activate hydrogen peroxide that operates at high pH include iron (III) tetra-amide macrocyclic ligands (TAML). A suitable example of a stabilizer for hydrogen peroxide at high pH is poly (α-hydroxyacrylic acid). Ammonia water is a particularly preferred solvent because ammonium bicarbonate, ammonium nitrate, and ammonium sulfate are produced as by-products as a result of NO _x and SO ₂ reacting with ammonia water. Since these products can be sold as fertilizer, the operating cost can be reduced. The basic chemicals for the all-in-one capture and by-product generation system are as follows.
SO ₂ capture:
_{NH 3 + H 2 O + SO} 2 → NH 4 + + HSO 3 - (1)
NH ₄ ⁺ + HSO ₃ + NH ₃ → 2 (NH ₄ ) + SO ₃ ^2- (2)
2H ₂ O ₂ + SO ₃ ^2- → H ₂ O + H ₂ SO ₄ (sulfuric acid) (3)
H ₂ SO ₄ + H ₂ O → 2H ⁺ + SO ₄ ^2- + H ₂ O (4)
2NH ₄ ⁺ + SO ₄ ^2- → (NH ₄ ) ₂ SO ₄ (ammonium sulfate) (5)
NO _x capture:
_{NH 3 + H 2 O → NH} 4 + + OH - (1)
H ₂ O ₂ + OH ⁻ → HO ₂ ⁻ + H ₂ O (2)
^{_{HO 2 - + NO → NO 2}} + OH - (3)
NO ₂ + NO ₂ → N ₂ O ₄ (4)
N ₂ O ₄ + H ₂ O → HNO ₂ + HNO ₃ (5)
HNO ₂ + H ₂ O ₂ → HNO ₃ + H ₂ O (6)
HNO _{3 ^{(aq) → H + + NO 3 -}} (7)
NH ₄ ⁺ + NO ₃ → (NH ₄ ) NO ₃ (ammonium nitrate) (8)
Hg capture:
H ₂ O ₂ + Hg ⁰ → Hg (II) + product (1)
H ₂ S capture:
_{H 2 S + H 2 O →} HS - + H 3 O + (1)
^{_{HS - + NH 3 + H 2}} O → NH 4 HS + OH - (2)

  <System process for removal of gaseous pollutants>

  One embodiment of the invention relates to a system including a nozzle array for gaseous contaminant removal. The nozzle array has a reshaped orifice plate (or nozzle plate) and includes fluid synthesis techniques that are compatible with a wide range of fluids and processing conditions. Pollutant gas removal is performed by passing the gas from a high surface to a volumetric gas-liquid contactor unit. The exhaust gas passes through a gas-liquid contactor having a substantially small contactor volume and airflow pressure drop in the horizontal direction (referred to as crossflow). A plurality of low-pressure, vertical flat jet arrays with aqueous-based solvent and substantial metal surface area run across the crossflow. By adopting an aerodynamic shape, the flat jet array forms a stable jet flow with less liquid particle contamination at a relatively high gas velocity.

  In preferred embodiments, sorbents suitable for gas absorption and removal have high liquid jet performance, high gas loading capacity, high oxidative stability, low reaction heat, low sorbent cost, low corrosivity, and marketable It is a system having characteristics such as a product stream. As discussed above, the jet nozzle plate configuration can be optimized in some 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 can achieve maximum jet performance (jet width, length, surface area) with minimal liquid pressure drop. An example of a sorbent is to contain 28% by weight ammonia and add a polymer additive or suspension to adjust the viscosity of the liquid to obtain the optimum jet width, length and thickness at the minimum driving pressure. 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 preferred to aid in the oxidation of the contaminant and thus the mass transfer kinetics. Examples of additives that promote the oxidation of contaminant molecules include, but are not limited to, Hg ⁰ and SO _2, hydrogen peroxide. Stabilizers are added to the sorbent mixture to avoid excessive decomposition of hydrogen peroxide at high pH. One example of a stabilizer for hydrogen peroxide at high pH is poly (α-hydroxyacrylic acid). The oxidizing power of hydrogen peroxide can be further improved by adding a hydrogen peroxide catalyst. An example of a hydrogen oxide 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 contaminant gases. The process is described from injecting exhaust gas 2600 into the gas-liquid chamber 2645. The gas plenum 2605 allows gas to flow evenly throughout the liquid flat jet. The liquid jet is generated by pumping the sorbent to the liquid plenum 2635 and spreading the sorbent across the nozzle orifice. The generated jet flows down vertically into the contact chamber 2645 and through the gas-liquid separator 2650 to the capture tank 2620. In the gas-liquid chamber 2645, the vertically flowing solvent intersects the gas cross-flow. The pollutant gas is absorbed into the sorbent liquid and removed from the exhaust gas stream. The cleaned exhaust gas 2655 is discharged from the outlet of the contact chamber. The sorbent is recirculated to continuously remove contaminants from the exhaust gas stream. Table 9 summarizes preferred embodiments of the geometric parameters of this embodiment.

  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 with respect to jet surface area (length and width) can be achieved by utilizing optimum additives to improve the viscosity / surface tension properties of the sorbent or by reshaping the orifice nozzle. However, for these tests, no polymer additive is added to the liquid sorbent.

Table 10 shows an example of operating conditions and performance of the gas-liquid contactor. Two sorbent systems, ammonia water and MEA, were tested under any operating condition. No additive involved in viscosity or oxidation is added to the sorbent mixture. Exhaust gas, the air and CO _2, usually CO ₂ dilution-air 1: Using those mixed with 9. The gas mixture was injected into the contactor under atmospheric temperature and atmospheric pressure conditions and measured using a calibrated mass flow controller. The volume flow rate of the liquid was measured by recording the amount discharged into the container on the receiver side where the liquid jet was calibrated at the measured time interval. The amount of the reduced (absorbed) CO ₂ is the percentage,% CO ₂ reduction _{= 100x (C in -C out)} / C in ... so expressed as (1), _{where, C in} and C _out is the concentration of CO ₂ entering and exiting the contactor. The relative amount of CO ₂ entering and exiting the contactor is determined by integrating the fundamental absorption band of CO ₂ near 4.2 μm with a Fourier transform infrared spectrophotometer (FTIR). FIG. 39 shows a typical FTIR absorption spectrum of CO ₂ in which a thin flat liquid jet containing liquid ammonia water is turned ON / OFF. An average of four test runs was run for each test result. The background CO ₂ concentration was recorded before each run. The test results for CO ₂ absorption under the described test conditions were such that CO ₂ removal exceeded 90%.

  <Pilot test at coal-fired power plant>

In this experiment, a trailer mounted 2 MW unit (10,000 ACFM airflow) was designed and manufactured for pilot testing at a coal fired power plant. Device systems include gas plenums, flue gas blowers, heat exchange sub-modules, gas-liquid contact modules including liquid capture and anti-splash sub-modules, demister sub-modules, nozzle array assemblies, sorbent pumps, liquid processing sub-modules, diagnostics and other Consists of accessory components. The system is designed to run in a closed loop steady state or batch configuration to meet drainage requirements for sewage containing preferential contaminants in power plants. Early pilot tests were conducted on the slipstream on a 0.13 MW scale (nominal 650 ACVM flue gas) to reduce time and risk. The 650 ACFM slipstream was diverted to the scrubber using two 6 inch steel pipes. The flue gas velocity in the contactor was matched to the power plant waste duct velocity (56 ft / s, 17 m / s) utilizing an 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 at a 5 psi hydraulic pressure drop, a minimum pressure drop of about 0.1 psi was observed in the flue gas. The emission of SO ₂ , NO, NO ₂ , CO, and CO ₂ flue gas was measured using a flue gas analyzer whose performance was verified by the Environmental Protection Agency (EPA). A slipstream was input to the unit at a temperature and pressure of 150 F and 11.2 psiA. 0.1 wt% of NaOH solution was circulated through the system to wash the SO _2.

  FIG. 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.

Referring to FIG. 36, the gas liquid contactor 3210 includes a flat liquid jet contact system as 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 flue gas exits from the flue gas outlet point 3250. In FIG. 38, a solvent pump 3260 is shown. FIGS. 39 to 40 are graphs showing the concentration of pollutants that are the target of combustion exhaust gas from a coal-fired power plant with and without using the Y-axis gas-liquid contactor in relation to the X-axis time. . A TESTO ₃ 35 electrochemical analyzer was utilized for all three analytical measurements. FIG. 39 shows the concentration of SO _{2 in} a first small scale test utilizing a contactor in flue gas, which is the equivalent of 0.13 MW. When the combustion exhaust gas was started, the SO ₂ concentration reached a substantially stable state at about 200 ppm. When the use of the contactor system was started, these SO ₂ emission levels immediately decreased to approximately the instrument detection limit and returned to a stable state. The TESTO instrument continued to sample the system with the contactor removed, indicating that the SO ₂ concentration increased rapidly towards the original contamination level. FIG. 40 is a diagram showing CO ₂ levels when different sorbents are used in the same mechanical system. The TESTO analyzer clearly shows that the CO ₂ level has been reduced and stabilized at that level within a 4 minute period.

Further deeper SO ₂ removal efficiency (> 99%) may be required for the purpose of pre-treating flue gas for meeting emission requirements and for efficient CO ₂ pollutant removal. The use of cleaning devices 0.13MW, about 99.5% removal efficiency of SO ₂ (an average of about 99%) that has been achieved is evident from Figure 39. As shown in FIG. 40, a scoping test for removing a plurality of contaminants using about 19% by weight of ammonia water was also performed. System is not optimized for CO ₂ absorption (low, short residence time), the unit has absorbed an amount greater than 50% of the slipstream CO ₂ under these conditions. In addition, more than 99.5% SO ₂ and more than 80% NO _x were simultaneously removed using aqueous ammonia. Due to jet and media optimization, it is envisioned that only two units are required to achieve 90% CO ₂ removal efficiency.

By rapidly scaling the results, we were able to demonstrate the operation of an approximately 2 MW (8400 ACFM) modular pilot scrubber that included parallel gas-liquid contact modules from the same power plant. The inlet channel area of the gas liquid contactor is about 3.9 ft ² , which provides a flow rate consistent with power plant effluent of about 58 ft / s (18 m / s) and a dwell time of about 0.07 seconds. To do. The solvent flow rate is 2800 GPM, providing an L / G of about 330 GPM / 1000 ACFM. The jet hydraulic drop was about 6 psi. The pressure drop across the contact stage of about 2 MW including the demister sub-module and the jet fill sub-module was 0.4 psi, where the pressure drop was about 0.1 psi with a jet fill of about 3.3 ft. The input and output combustion exhaust gas temperatures were 250 degrees Fahrenheit and 115 degrees Fahrenheit, respectively. A stable state (without solvent discharge) 24 hours test was performed average SO ₂ cleaning efficiency at 99%.

FIG. 41 shows a large scale test for SO ₂ capture where a uniform flue gas stream of about 2 MW passes through a larger contactor. Multiple ON / OFF cycles were performed to ensure consistent operation. FIG. 41 is a graph showing the results of cleaning SO ₂ by the 2 MW scale using H ₂ O and NaOH (0.1 wt%). The graph shows time (hours) on the x-axis and concentration on the y-axis with the unit of ppm. As shown, the combustion exhaust gas is emitted as pollutant molecules in SO ₂ above 350 ppm. Gas-liquid contact module to remove substantially all of the SO _2. More specifically, when the contactor liquid jet was interrupted to test whether it was reproducible, the SO ₂ concentration returned to a value exceeding 350 ppm as shown in FIG. When the use of the liquid jet module was started, the SO ₂ concentration dropped to near the reference value. Repeating this consistently produced the same results as shown in FIG. Furthermore, SO ₂ removal efficiency was confirmed by recent follow-up testing. In addition, a simulated sewage treatment experiment using a consumption medium was performed in the laboratory to prove the precipitation of calcium sulfate.

Embodiments of the present invention include a modular gas-liquid contactor, or a gas-liquid that includes a post-combustion technique that removes multiple flue gas pollutants (SO _x , NO _x , CO ₂ and particles) over a wide range of flue gas conditions. Concerning contactors. Wet cleaning systems are subject to mechanical outages due to failure to comply with mechanical or release regulations. The gas-liquid contact cleaning system is designed as a small footprint package for continuous online processing with excellent performance, flexibility, convenience and reliability.

Although actual performance metrics (eg, SO ₂ removal) are directly comparable to conventional methods and equipment design, the process equivalent of the present design, method, and system is useful in achieving these results. It is surprising that the size is less than half that of the conventional system and the cost is more than 10 times smaller than the capital cost of the conventional system.

  Use modular design method for manufacturing and scaling of modular gas-liquid contact cleaning unit. By adding cleaning modules in parallel or in series, the required contaminant removal performance is achieved. This is achieved by a low pressure drop (eg, a pressure drop of about 0.4 psi) and a low parasitic power requirement (eg, less than about 0.8% per stage). This method standardizes manufacturing and allows customization of cleaning equipment for each site requirement. The modular gas-liquid contactor is manufactured in an assembly line manufacturing process in a factory.

  <Gas-liquid contact module>

  FIG. 42 represents a 60 MW cleaning unit and support structure. FIG. 43 is a front view of a section of the 2 MW section of the wash tower of FIG. FIG. 44 is a side view of a section of the 2 MW section of the wash tower of FIG. FIG. 45 shows the arrangement of inlet channels and jet filling zones. In this embodiment, the system is configured to have a dimension of less than about 600 lbs and about 5 ftx10 ftx10 ft. These units may further be capable of handling flue gas streams greater than about 85,000 cfm and can be scaled as appropriate.

  The units are designed to be stacked in parallel and sized according to the power plant. In some parallel configurations, the modules may be configured on top of each other or next to each other. The input gas stream is divided (for example, equally) between the parallel modules so that each module can perform equal processing. In one embodiment, 10 2MV base modules are stacked vertically to produce a 20 MW composite module (85,000 cfm). Then, the three 20 MW modules are connected in the horizontal direction to generate 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 by pumping 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 provides a primarily planar liquid jet, each liquid jet including a planar sheet of liquid, and the plurality of liquid jets are located substantially in respective parallel planes. A flat liquid jet is formed in the wash tower 3345 where the gas stream 3320 passes parallel to the flat surface of the jet. As the sorbent falls to the bottom of the tower, the heat exchanger 3340 captures the heat absorbed by the sorbent in the contact process. The sorbent then flows from within the conduit 3335 to the pump housing 3330, from which most is further pumped to the water treatment system 3325.

  The water treatment system shown at 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 trapped gas phase molecules and fit into the “box” of FIG. On the other hand, large systems may include precipitation tanks, settling tanks, and solid compression subsystems that may be large depending on the chemicals and applications utilized.

  The pump housing, shown at 3330, may be a liquid pump of a size suitable for an application that supplies an appropriate volume of liquid to a contact system known in the art. The block shown at 3330 may be optional and determines the site environment and pump selection and whether to provide the selected pump depending on whether it needs to be protected from rain or snow.

43 to 45, the structure of the spray back base unit is shown. The base unit or base module of this embodiment has an input channel of about 25 cm × 130 cm and about 1.7 m ² containing about 5 sprays / cm ² based on all 3400 nozzles (40 rows of 85 nozzles) of the spray pack. Consists of spray pack area. FIG. 43 shows a waste liquid inlet 3360, a waste liquid outlet 3350, and a jet filling zone 3355. The jet filling zone 3355 is the actual contactor volume where the liquid jet and gas molecules contact each other. In FIG. 45, a side cross-section of the jet wash fill 3365 is shown followed by a spray or demister 3370 to prevent fluid contamination from the waste stream. Even if the liquid jet is fast, some distillation of the liquid gets mixed into the airflow, especially when the gas velocity is high. This contaminant includes small droplets (eg, aerosol or mist). The demister includes small zones through which small mist droplets pass through the zone containing the element represented by 1660 in FIG. 29 and is condensed on the surface of these elements and flowed back to the liquid bath system. In this particular embodiment, the elements are vertical rods, but can include any design that causes a small pressure drop and can combine condensation / merging surfaces and turbulence (eg, mesh, thermal Including but 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 present invention. FIG. 47 shows the configuration of the nozzle plate in 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. Systems (eg, gas-liquid contactors or cleaning units) are designed with a snap-on nozzle array that includes an orifice plate and can replace worn or clogged orifices without interrupting operation. The system can further be designed to provide overlap to the mechanical equipment or support system. For example, a large plant facility can include approximately 20% of the spare concept so that parallel units can be repaired when necessary without interfering with plant operation. Referring to FIG. 46, a partially removed position of the removable plate 3410 is shown. Removable plate 3410 includes a plurality of nozzle plates having a plurality of rows of nozzles forming a plurality of 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 removed. FIG. 48 shows a sealing mechanism 3440 designed to seal the jet plate 3425 with an elastomeric seal 3430 against the sealing surface 3435. Shown are a small cross-sectional side view 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 3415 and the end of 3415 has a series of small angled grooves in which pins 3440 attached to frame 3435 fit into grooves 3445. . The angle of the groove 3445 is configured such that the angle of the groove functions as a cam for the pin 3440 and pressurizes the elastomer seal 3430 by torque generated in the sealing direction. While this is merely one specific embodiment, it will be apparent to those skilled in the mechanical systems art that fluid level sealing is a readily conceivable alternative that performs a similar function.

<SO _x , NO _x , and modular gas-liquid contactor in particle process>

Another embodiment is a Na / Ca dual alkali comprising a compact, high performance, low cost, low water, energy efficient gas / liquid contact or cleaning system with advanced sewage and product flow treatment capabilities It relates to the analyzed design for deep flue gas SO ₂ removal using the process. Table 11 shows the design requirements for this process.

  <Combustion exhaust gas control system>

  Methods used in applications for treating flue gas using an embodiment of the present invention can be described using general terms. These generalizations can be customized according to site and usage requirements, but can be divided into four main sections. FIG. 49 is a process flow diagram of the contaminant removal system. In FIG. 49, the basic process flow diagram of the gas-liquid contact system shows the main system components and the main stream points. The four sections are: section 1: flue gas or process gas section, section 2: scrubber or reactor section, section 3: sorbent or reactant input, and section 4: reactive biological treatment and sorbent recycling ( Or release). From the gist of the present embodiment, these four sections will be described in detail by taking the use of flue gas for desulfurization as an example. However, a person skilled in the art can make a high-efficiency gas-liquid contact system by further modifying these processes You will come up with a number of different processes that can benefit from.

Referring to section 1, flue gas 5402 is generated and released by an industrial process (such as a coal-fired power plant). The flue gas enters section 2 at process point 1 (PP1), the flowing gas is processed in section 2, then passes through PP2, is heated appropriately 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 exhaust gas may contain multiple pollutants depending on the fuel source and the efficiency of combustion. In this embodiment, it is assumed that only SO _x , NO _x , H ₂ O, SO ₂ , HCl, and HF are formed in the boiler that supplies the reaction system shown in FIG. Between the production and release of flue gas 5402, the flue gas stream slip stream (part or all) is redirected to pollutant reduction or to the cleaning system (eg, sections 2-4).

Section 2 includes a gas-liquid contact modular assembly 5408 that functions as a scrubber or reactor in accordance with various embodiments of the invention. In this section, _SO 2, HCl, HF, and some NO ₂ is removed from the flue gas when using the chemicals shown in FIG. 49. The efficient removal of CO ₂ from this flue gas stream and the chemical shown in FIG. 49 is negligible and may improve dramatically depending on the chemical used and the pH of the sorbent. In an embodiment, it is assumed that little CO ₂ is captured. Contactor 5408 captures SO ₂ , HCl, and HF. The fluid containing the liquid of the liquid jet is an aqueous solution. This aqueous solution mixed with gas is captured by the capture tank 5410. In Section 2, the captured fluid is recirculated with a recirculation pump in PP6. This recirculated fluid slip stream is withdrawn using process valve 5418 to perform the secondary treatment of section 4.

  Section 3 is a sorbent and solvent replenishing fluid section configured to adjust chemical activity, liquid pH, and replenish reactants. Any liquid lost due to evaporation is replenished with PP7 by a local water source 5412. The liquid is built at a relatively high pH (value above 7) and is maintained at this level with PP8 by NaOH source 5414, or once the soluble sulfite concentration has reached a more stable state, section 4 The pH can also be maintained by adding lime 5416.

Section 4 describes dissolved or reacted gas phase molecules as solid products (eg CaSO ₄ ), solid soil (eg CaSO ₃ ), other available products (eg fertilizer / NH ₄ SO ₄ or NH ₄ NO ₃ ) is a secondary treatment section that chemically changes or mineralizes. The process liquid is transported from section 2 to PP 12 at precipitation tank 5420 and lime / Ca (OH) ₂ 5416 is added at PP 15 to raise the pH and provide Ca ²⁺ to provide SO ₃ ²⁻ (or completely). React / precipitate with SO ₄ ^2- in oxidized mode. The resulting CaSO ₃ mixture flows into the settling tank 5422 at PP16 and is stored after settling in the slurry holding tank 5424. When a sufficient amount of CaSO ₃ is captured, it moves to the filter press 5426 to remove the liquid, passes through the PP 29 and moves to the salt water holding tank 5428. The solid 5430 from the filter press 5426 is either processed in a garbage disposal site or sold as a gypsum / sheet lock CaSO ₄ for tertiary processing. The liquid from the brine tank 5428 is moved at PP26 in a softening step 5432 for recycling or regeneration to remove excess Ca ²⁺ and added soda ash (Na ₂ CO ₃ ) 5434 to remove Na ⁺ . To be replenished. The regenerated sorbent is sent back to section 2 at PP3 via secondary process valve 5436.

In the particular embodiment of FIG. 49, a 20 MW system draws a portion of the flue gas from a 140 MW coal fired power plant. Combustion exhaust gas is generated by burning coal with low sulfur content (eg, from the Powder River Basin, Wyoming). Specific attributes to be considered in this embodiment are shown in Table 12. The combustion of the coal produces approximately 350 to about 400 ppm of SO ₂ in the flue gas, which is a major contaminant for this example system. Other contaminants 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 indicated also at process point 1 (PP1). The temperature of the flue gas entering at PP1 ranges from about 250 degrees Fahrenheit to about 300 degrees Fahrenheit and comes from the power plant fly ash baghouse. The fly ash baghouse serves to remove bulk fly ash generated from coal combustion and further reduce the temperature to the consistent range described above. The water concentration of this flue gas ranges from about 6% to about 8% by mass.

At PP1, the flue gas slip stream enters section 2 (cleaning section). The combustion exhaust gas flows through the gas-liquid contactor 5404 at a gas velocity of approximately 10 m-second- ¹ . Here, the gas-liquid contactor will be described. Sorbent liquids utilized is sodium sulfite which is formed in the first initial reaction between NaOH and SO _2. A 50% by 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 processing, and this pH can be maintained at about 6.5 as appropriate. During start-up, water can be somewhat absorbed SO _2, thereby to pH value drops rapidly, it becomes an acidic aqueous solution. Thus, NaOH serves to maintain pH approximately neutral and provide Na ⁺ as a counter ion for SO ₃ ²⁻ . The following equation shows the main reaction of interest for this system that removes SO ₂ .
SO ₂ + H ₂ O → 2H ⁺ + SO ₃ ^2- (1)
2NaOH + 2H ⁺ + SO ₃ ^2- → 2Na ⁺ + SO ₃ ^2- + 2H ₂ O (2)
During steady state processing, this is a sodium sulfite solution that will react effectively with SO ₂ to a concentration of about 0.5M and the reaction forms sodium bisulfite in water. The chemical formula representing the total reaction is as follows:
Na ₂ SO ₃ + SO ₂ + H ₂ O → 2NaHSO ₃ (1)

The flue gas exiting the contactor has been 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 in the module removes excess moisture. When the flue gas exits the SO ₂ depleted gas-liquid contactor region (PP2), it may optionally be heated by the flue gas heater 5404 (up to a temperature well above the dew point) and passes through the ID fan 5440 to discharge the flue gas. Released into the stack 5406. Other options for flue gas control include using gas to the air heat exchanger to convert to a wet stack configuration, or using power plant process steam for reheating. In some cases, waste heat from the entire sorbent treatment system can also be used because hot desorption gas is useful in reheating the flue gas in a thermal desorption step after leaving the stripper. . The continuous processing of the gas-liquid contactor 5408, leading to the construction of sodium bisulfite, the absorption efficiency of SO ₂ is reduced unless the removal of SO ₂ reaction product. Accordingly, the slip stream (PP12) of the section 2 liquid sorbent recirculation system is continuously drawn to the secondary chemical treatment system.

In the secondary processing system shown in Section 4, SO ₂ is completely mineralized to form a solid product calcium sulfite (PP16). Calcium sulfite is later filtered (PP18) to remove excess water and appropriately treated in a garbage disposal site (PP24). Lime (Ca (OH) ₂ ) serves to mineralize the sulfurous acid into a solid precipitate (PP15) and maintain the pH at an appropriate level as an alternative to additional NaOH additive to the sorbent loop. The reaction performed in the secondary treatment is as follows.
2Ca (OH) ₂ + 4NaHSO ₃ → (CaSO ₃ ) ₂ H ₂ O + 2Na ₂ SO ₃ + 3H ₂ O
The calcium scale problem is diverted to the filter press process (PP32) using a standard ion exchange process that utilizes sodium carbonate (dissolved in water—PP31) in a later “softening” step (PP26). By forming calcium carbonate (which does not dissolve at this pH), it can be avoided by removing excess calcium. In this same step, sodium thiosulfate can be added (PP34) to inhibit oxidation of sulfite (SO ₃ ²⁻ ) to sulfate (SO ₄ ²⁻ ). This process also serves to regenerate Na ₂ SO ₃ which is the primary SO ₂ capture reagent.
CaSO ₃ + Na ₂ CO ₃ → CaCO ₃ + Na ₂ SO ₃
After softening and regeneration of the active sorbent chemical, it is recycled back to the main contactor process loop (PP33).

<SO ₂ and process module removal system>

The size of the process analysis and gas-liquid contactor cleaning and absorption system is determined based on the design parameters in Table 12.

The gas-liquid contactor (absorber) is operated in a continuous, steady state mode utilizing a side-popular flat jet spray nozzle. Absorber, a minimum of water, the reactor volume, show that pressure drop, and that the SO ₂ removal efficiency in the contact time can be performed with high volume mass maximizing movement (Kca~64s ^-1).

  The absorber exhibits a low gas side pressure drop and a low liquid side pressure drop that translates into low power consumption. The pressure drop at the liquid jet orifice is less than about 10 psi, which can greatly reduce fluid power requirements during operation. The 28,000 gpm liquid pump that circulates the solvent constitutes the bulk power consumption in the absorption loop. The power draw P (kW) is “.75 × flow rate (gpm) × ΔP” / “1714x pump efficiency”, about 150 kW for a pressure drop of about 8 psi (or about 20 MWe of power draw), about 28, The pump efficiency is about 65% at 000 gpm. The pressure drop on the gas side in the flat jet system is as low as about 0.1 psi per 3.3 ft filled jet (2.7 in WC).

In comparison, the average pressure drop of the related art packed tower is about 1.0 inch of H ₂ O with a 1 foot fill, or about 10 inches of H ₂ O with a normal 10 foot absorption bed. It is. Compared with the prior art, the gas-liquid contactor consumes less power and the absorber can operate at a higher L / G ratio (330 gallon / 1000 ACFM), so that of the conventional absorber (L / G90-130) higher removal efficiency is achieved.

Absorption systems can capture heavy metals, chlorides, and fluorides as well as capture contaminants of interest (eg, SO _x , NO _x , and particulate matter) from flue gas. The particulate material is mostly fly ash carried from a baghouse of 2.5 μm or less. Metals and halides are derived from coal and depend on the type of combustion coal. All these constituents are removed from the absorption loop of the solvent treatment system. The molar flow rate from all constituents in the flue gas to the absorption loop is equal to the molar flow rate of these pollutants in the absorption loop of the solvent treatment system and therefore exits the solid and brine streams. The concentration of all constituents in the absorption loop reaches a stable state.

Gas solubility, solvent temperature, and pH also play an important role in contaminant absorption. The system of this embodiment operates at a relatively low liquid temperature (eg, about 100 degrees Fahrenheit to about 125 degrees Fahrenheit) to optimize gas solubility and minimize solvent evaporation. Soluble equilibrium point between the gas phase _{p a} and the water phase _{C a} contaminant (300K) is given by Henry coefficient _K H ₌ C a / _{p a.}
SO ₂ (g) → H ₂ SO ₃ , K _H = 1.4M / atm (1)
^{_{H 2 SO 3 → H + +}} HSO 3 -, K 1 = 0.014 M (2)
^{_{HSO 3 - → H + + SO}} 3 2-, K 2 = 7.1 x 10-8 M (3)
^{_{HSO 3 - + 1 / 2O 2}} → SO 4 2- + H +, k> 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 = [SO ₂ ] + [HSO ^{3 −} ] + [SO ₃ ²⁻ ] And S (VI) is the sum of all sulfur in the +6 oxidation state, and [S (VI)] _tot = [SO ₃ ] + [HSO ₄ ⁻ ] + [SO ₄ ²⁻ ]. , And. Since SO ₂ gas dissolves in water, the solute is converted to bisulfate (HSO ₃ ⁻ ) and sulfite (SO ₃ ²⁻ ) products according to the equilibrium point governed by K _H , K ₁ and K _2. . This process depends on the pH when the H ⁺ product is formed. As more H ⁺ is produced (pH drops), the equilibrium point shifts back to reactant production. At pH values below 3.5, a considerable amount of SO ₂ is evacuated from the solvent. To optimize the removal efficiency and cost of the SO _2, it is added sodium hydroxide in a stable state, or needs to maintain the other chemical base in the vicinity of about 6-7 pH of the system by injecting into the solvent loop is there.
SO _{2 (g)} + 1 / 2O _{2 (g)} + 2NaOH (aq) → Na ₂ SO ₄ (aq) + H ₂ O (1)

  <Sulphite oxidation system>

  The forced oxidation of sulfite to sulfate can be done with a simple air sparger (using a 14 kW air compressor) in a separate tank. The sparger is simple, but the gas-liquid contact efficiency is low, so the air flow rate is set to about 3 times the stoichiometric amount required for complete oxidation. Assuming 100% oxidation, about 533 lb / hr of sulfite is oxidized to sulfate. In a full scale system, it would be cost effective to use an additional highly efficient gas-liquid contactor instead of a sparger.

  <Solvent treatment system>

The design criteria for sulfate precipitation and removal when the system is run in full oxidation mode (as is the case with most sulfur and sulfate (SO ₄ ²⁻ )) are shown in Table 13. The system is designed for <50 ppm HSO ₃ ⁻ and 14.4% SO ₄ ²⁻ in the operating liquid at steady state. The flow rate of the solvent process stream is directly dependent on the SO _x steady state loop concentration, which determines the size requirements in the design of the solvent process system.

  <Advanced design, sorbent and process options>

Table 14 shows 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.

The choice of sorbent / sorbent treatment / disposal system is driven by performance, reagent costs, and site byproduct disposal requirements. The result of comparison of reagents is best utilized in SO ₂ removal in the packed tower with respect to the reaction and the operating costs are shown in Table 15.

Caustic and ammonia based systems, but has the potential for the highest reactivity and deep SO ₂ removal, has the disadvantage that the cost will be higher. The cost of these reactants is greatly offset by a dual loop process where the solvent can be recycled back to the absorber. Among all the possibilities, the most promising is the NaOH / Ca (OH), NaCO / Ca (OH), NH / Ca (OH) dual loop. Fly ash has the potential to reduce reagent costs to zero, but is at the highest risk.

A Na / Ca dual loop is preferred, but an NH / Ca dual loop is also a possible option. It has the advantages of a highly reactive and soluble sorbent, a clear contact solution, and a sorbent treatment loop that can recycle relatively expensive ammonia. The advantage of ammonia over sodium is that the return loop does not contain calcium or other contaminants that can scale the absorber because the precipitation step separates ammonia as a gas. In addition, the gas-liquid contact system in embodiments of the present invention can utilize ammonia for both purposes when combined with a CO ₂ absorption system. This is because ammonia is volatile and an additional (small) cleaning unit can be placed in the flue gas vent line to prevent ammonia from slipping into the stack.

Since fly ash is alkaline and easily available, it may be used as an FGD absorbent. 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 properties of the FGD slurry being contaminated downstream and difficult to process. See Kohl et al., “Gas Purification”, Gulf Professional Publishing, 5th edition, 1997, incorporated herein by reference. However, fly ash is carefully prepared (eg at the optimal SO ₂ —CaO / MgO chemistry stoichiometric level) to prevent cementitious reactions within the gas-liquid contactor itself, thereby allowing the fly ash to function as a fly ash. May be performed under conditions that do not impair the cleaning operation. Alternatively, a similar reaction of these C _a / Mg may be desirable and can be used to produce a cementitious material as a commercial product within the sorbent treatment area. In addition, if it is desired to turn the by-product dipsum into a product, a disposal scheme that separates the solvent treatment system and fly ash from the dipsum is desired.

  <Overview of the system>

Na / Ca dual alkaline contact processes and systems have the advantage of higher technical and economic performance over conventional systems. Table 17 summarizes the main basic performance parameters of the contact system and the typical (per MW) system for the 20 MW case of this embodiment.

Deep SO ₂ removal requires fast and efficient mass transfer kinetics, for which the use of NaOH is suitable. A system utilizing calcium hydroxide / calcium carbonate is a low cost solvent, but also a low reaction solvent. Ventilator Im / Limestone based absorbers that increase reactivity can be operated with slurry (solid). However, the solids are susceptible to absorber surface scaling (due to the formation of calcium sulfite / calcium sulfate) and in some cases may further hinder mass transfer. The significant cost savings associated with utilizing Na / Ca is due to the re-requirement of 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 sulfur-rich fuels such as those in Kohl et al. “Gaseous Purification”, Gulf Professional Publishing, 5th edition, 1997, incorporated herein by reference) Then). The cheapest reagent is calcium (Ca (OH) ₂ ), which is used to precipitate gypsum (product by-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 much more efficient gas / liquid contactor can be operated. The disadvantages are increased complexity and the need for two reagents. In contrast, in a single loop wet limestone FGD process, all the necessary steps are performed in a single vessel, which refers to dissolving the lime storm as calcium carbonate, Gas-liquid contact is performed, SO ₂ is absorbed, reacted with calcium, oxidized, and precipitated. This results in a single, relatively simple system. Disadvantages are that the slurry is susceptible to corrosion / abrasion and 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 major equipment components in the contact systems described here above 20 MW and over 200 MW. In these embodiments, it is assumed that an exhaust blower (ID fan) for combustion exhaust gas is already arranged and cannot be counted. Connect the bulk power draw to the solvent recirculation pump. The contact system operates from low liquid side fluid and with mechanical stress due to the large (> 10X of conventional spray nozzle) flat jet orifice area. In this embodiment, the described 20 MW liquid pump (28,000 GPM) draws significant power from the system due to the efficiency of the intermediate pump (˜65%). Take advantage of the larger liquid pump (> 100,000 GPM) available in full scale operation (> 200 MW) as it would be much more efficient (˜85%). A fairly low (1.7X) low parasitic power load will be achieved.

<CO ₂ process gas liquid contactor>

These advantages allow for the achievement of environmental targets of CO ₂ removal efficiency (> 90%) and energy cost (<20%), including a small, low cost, low pressure drop, and high energy efficient cleaning system. Proven in terms of cost and energy saving process. Three possible absorption / regeneration reaction methods utilizing ammonia solutions are described in Yeh et al., “Fuel Processing Technology”, Volume 86, 14-15, pages 1533-1546, October 2005, This is incorporated herein by reference.
2NH _{3 (aq)} + CO _{2 (g)} + H ₂ O → (NH ₄ ) ₂ CO _{3 (l)} , Delta H _r = -24.1 kcal / mol (-986 BTU / lb CO ₂ ) (1)
NH _{3 (l)} + CO _{2 (g)} + H ₂ O → NH ₄ HCO _{3 (l)} , Delta H _r = -15.3 kcal / mol (-622 BTU / lb CO ₂ ) (2)
(NH ₄ ) ₂ CO _{3 (l)} + CO ₂ + H ₂ O → 2NH ₄ HCO _{3 (l)} , Delta H _r = -6.4 kcal / mol (-262 BTU / lb CO ₂ ) (3)

The reaction is exothermic because it is described in terms of absorption. The most energy efficient method of CO ₂ capture and solvent regeneration is the carbonic / bicarbonate reaction in equation (1). Since the absorption reaction is desirably performed at a low temperature, the cleaning device liquid is cooled to 90 degrees Fahrenheit, and the stripper liquid is heated to 140 degrees Fahrenheit to release CO ₂ gas at 1 atm. Utilizing carbonic acid / ammonium bicarbonate chemicals can significantly reduce operating costs compared to utilizing alkanolamine-based solvents because their energy of formation is less than half that of EMA.

<Analysis of the flow of the gas-liquid contact process diagram and CO _2>

FIG. 50 is a process flow diagram from a contaminant removal system in another embodiment. First, flue gas enters the contactor to remove contaminants such as SO _x , NO _x , and particulate matter. It then enters a CO ₂ absorber where it is contacted with, for example, a chilled ammonium carbonate solution or piperazine, and most of the CO ₂ is captured as ammonium bicarbonate or as piperazine carbamate, respectively. Other amines, alkanolamines, and / or bases (eg, KOH, NaOH, etc.) are also available in this loop. The chemical system utilized is an ammonium hydroxide / ammonium carbonate system where the ammonia in the cooler is mixed into the flue gas as an ammonia slip and transported to an ammonia scrubber for removal.

The cleaned flue gas is conveyed to a condensation heat exchanger where it is heated to a temperature above the dew point of about 40 degrees Fahrenheit and then discharged from the stack. The ammonium carbonate / ammonium bicarbonate absorption stream is recycled back to the scrubber after being recirculated with a cooling device and heat pump. By removing the side stream of the absorption solution, from overheating, back to the stripper, to release the captured CO _2. The dilute solution returns to the absorption loop. The stripped CO ₂ is transported some water vapor and ammonia, which is removed during the compression in the condensing heat exchanger. Moisture and ammonia are returned to the absorption loop. The washed CO ₂ is sent to the compression train and sequestered. Major energy savings process step is to cool the ammonium carbonate absorbent solution using heat pump, by away the heat from the solution of the stripper, is performed by separating the CO ₂ to raise the temperature. By using a heat pump to capture the energy of the absorbing stream and send heat to the stripper stream, about 10% of parasitic power can be saved.

Table 20 shows the system size and analysis design criteria. The process is divided into six main process sections as shown in FIG. 50, specifically, section 1 is a flue gas regulation system, section 2 is a CO ₂ absorption loop, and section 3 is a CO ₂ stripper loop. Section 4 is an ammonia or amine slip loop, Section 5 is a cooling system and Section 6 is a CO ₂ compression train. All flow rates and heat loads are calculated for the system shown at 20 MW.

  <Combustion exhaust gas control system>

In this embodiment shown in FIG. 50, the flue gas regulation system includes an inlet 5002 and an outlet 5006 as the flue gas enters the optional heat exchanger / cooling device 5004. The flue gas conditioning system receives a gas that may have already undergone some treatment (eg, removal of SO ₂ , HCl, or other acid gases). The heat exchanger / cooling device 5004 can be optional since it is known in the art to depend on the incoming gaseous components and the chemistry of the absorber (eg, ammonia / ammonia carbonate). If so, a cooling device is required). The flue gas is cooled to clean the SO ₂ (eg, with a contact system (not shown) in one embodiment of the invention). In the present embodiment, the combustion exhaust gas 5002 contains contaminants such as CO ₂ , N ₂ , H ₂ O, O ₂ , and other rare gases.

<CO ₂ absorption loop>

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

In operation, the flue gas containing CO ₂ is directed through the inlet 5014 of the gas-liquid contactor 5008 to separate a portion of CO ₂ . The Section 2 CO ₂ absorption loop includes 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 absorbent solution carries an additional amount of CO ₂ to capture tank 5010 as part of the recirculation loop.

In this embodiment, the energy requirements of the CO ₂ absorption loop are handled by section 5 heat exchanger / cooling device 5012. The general chemistry described herein, which utilizes ammonium carbonate, amine, or alkanolamine, absorbs CO ₂ better when cooled to temperatures below the flue gas temperatures found in normal systems. The Thus, if necessary, section 5 heat exchanger / cooling device 5012 can provide a cooling function to maintain optimal operating conditions for the absorbent solution.

<CO ₂ stripper loop>

Section 3 includes an inlet 5016 connected to a heat exchanger / cooling device 5018 having an outlet 5020. The outlet 5020 is connected to the gas-liquid contactor 5022. The gas-liquid contactor 5022 has an outlet 5024 connected to a capture tank 5023 having a recycle loop. The gas-liquid contactor 5022 is configured to remove the captured CO ₂ from the absorbing solution. The CO ₂ strip treatment can be performed by several means (eg pressure fluctuation, pH adjustment, or heating of the CO ₂ / absorbing solution). The components of section 3 can be changed depending on the method selected. In any case, it is advantageous to capture the absorption solution after the release of CO ₂ and recirculate the absorption solution to the main absorption loop of section 2. The output of section 3 is sent to stack 5034.

<NH ₃ / PZ absorption loop>

Section 4, the ammonia or amine absorption loop, is designed to capture ammonia or amine slip from the flue gas exiting the CO ₂ absorber 5008. This treatment is unique when it contains NH ₃ according to the temperature of the absorbent solution (the colder the less slip). The NH ₃ / PZ absorption loop includes a gas liquid contactor 5026 connected to the inlet 5024. The gas liquid contactor 5026 includes an outlet 5028 connected to the capture tank 5030, a recycle loop, and an outlet 5032. If amines such as piperazine or alkanolamine are utilized as the absorbing solution, the implementation of this section can be determined by examining the overall process requirements and temperature, since there is less need to provide section 4. This section 4 can be an optional process because the smaller molecular weight amine slips and the higher molecular weight amine does not slip, so there is no need to process. Output 5032 may be sent to flue gas stack 5034.

<CO ₂ compression train>

Section 6 shows the process area where CO ₂ is stripped from the absorbing solution. The CO ₂ compression train includes a compressor 5036 coupled to a gas liquid contactor 5022. This section is configured to capture and pressurize pure CO ₂ from the gas liquid contactor 5022. In other words, after this section, it is desirable to carry out secondary recovery (EOR) of crude oil, sequestration of metal ions, and other secondary steps to transport in a convenient manner for secondary industrial use. One of these options may include a method of compressing CO ₂ with a compression train and isolating it at supercritical pressure to form liquid CO ₂ that is transported to the end use by truck or pipeline. it can.

<Other solvent systems for CO ₂ capture>

In sections 2 and 3 of FIG. 50, various sorbents can be utilized for CO ₂ capture and / or stripping. The sorbent may comprise an ammonia carbonate based solvent selected as the base solvent. However, the system does not include cleaning solvents containing amines such as ammonia, diethanolamine (DEA), and monoethanolamine (MEA), and promoted carbonates, piperazines, tertiary or inhibited amines (methyldiethanolamine ( (MDEA) and 2-aminomethylpropanolamine (AMP), metal organic framework and molecular encapsulation).

The CO ₂ system embodiments present some of the strengths and advantages of post-combustion CO ₂ capture. For example, a very large contact surface area becomes available with a small contactor volume. This leads to economic savings in two areas, where a small footprint means less capital costs, and a low pressure drop on the liquid side means less operating costs. It shows that it can be done. Lower capital and operating costs increase the range of possible CO ₂ sorbents. For example, if an inexpensive sorbent has a low reaction rate and requires a large contact area (eg in the case of seawater or deep saline aquifer), it is still a practical method for CO ₂ gas-liquid contact systems, Ordinary standard gas-liquid contactors (eg bubble or spray towers) will not normally be considered.

In most mature CO ₂ capture systems for flue gas, alkanolamines and ammonium carbonate / ammonium bicarbonate (AC / ABC), the maximum energy consumption is related to the heat of reaction. Energy involved in AC / ABC reaction consumes about 70% of the total energy required to absorb desorption of CO _2. ABC solution, must be cooled to 55 degrees Fahrenheit in order to absorb CO _2, it is necessary to heat it to 265 degrees Fahrenheit to release the stripper. Options to achieve energy reduction include two factors. That is, to find a system having a small reaction heat during absorption and desorption of CO ₂ , or to divert the heat released during absorption to the desorption reaction. Ammonium carbonate / ammonium bicarbonate is currently the lowest energy chemical sorbent. Physical solvents require almost no regeneration energy but work best at high pressures. Membrane systems can divert absorbed energy to the desorption process, but are currently only used in small systems. In the following, alternative processes that can be used to capture CO ₂ from flue gas are classified and described.

In searching for an alternative CO ₂ absorption system, the sorbent must match the technology used. Three post-combustion absorption technologies have been developed: a gas-liquid contactor, a dry contact system, and a membrane contact system. A gas-liquid contact system requires a liquid sorbent. The gas-liquid system divides absorption and desorption into two separate process steps and takes place in two separate containers at different pressures and temperatures. This system is typically energy consuming both in the steps of cooling to absorb heat and heating to absorb heat. This process requires varying temperatures and / or pressures and requires a lot of energy. A dry regeneration sorbent system using sodium bicarbonate is the same process as a gas-liquid contactor except that the sorbent is a solid phase.

But the membrane system is fundamentally different. A membrane-based membrane is a very thin septum made of a permeable material that separates two streams and may be a solid or liquid held in a sponge-like material. The membrane is designed to select the gas to be separated. Whether the membrane material is solid or liquid, the membrane absorbs CO ₂ on the concentrated side and moves it to the dilution side where CO ₂ is desorbed. The driving force is a concentration gradient of CO ₂ across a very thin membrane. The aesthetics of the membrane system is that absorption and desorption can be performed in the same container, at the same temperature, and almost the same pressure. Absorption and desorption are performed within a few microns of each other in a very thin membrane, so that the absorbed energy can be transferred to the desorption reaction at a constant temperature. Therefore, the entropy change is zero and the required net energy is zero. Liquid in the membrane can be chosen so that it is possible to carry selectively CO _2. Disadvantages are manufacturing costs, membrane life, very clean flue gas requirements, and enormous contact area (about 1 million square meters for the entire commercial system). It is necessary to channel the combustion exhaust gas of hundreds of thousands of ACFM that enters the duct up to a cross section of 100 m ² into billions of fibers with a cross-sectional area of each fiber of 60 nm ² .

Alternative solvent systems available for post-combustion absorption in gas-liquid contactors include chemical and physical ones. Wet chemical sorbents include amines, carbonates, accelerators, hybrids, and pH fluctuations. Wet physical sorbents include metal organic frameworks, ionic liquids, seawater, and underground brines. Glycol is a high pressure system and will not be described because it is more suitable for absorption before combustion. Celexol is an example of a commercial glycol system currently used for cleaning natural gas and is a high pressure process. Each wet sorbent available for the CO ₂ gas-liquid contactor is described below.

Hydrous amine is the current state of the art for CO ₂ capture in power plants recognized by those skilled in the art. Amine sorbents include ammonia (NH ₃ ), monoethanolamine (MEA), methyldiethanolamine (MDEA), 2-minomethylpropanolamine (AMP), PZ piperazine (PZ), and others. All react first with CO ₂ (CO ₂ + 2RNH ₂ ⇔ RNH ₂ COO ⇔ RNHCOOH) to produce amine carbamate. In addition, amine and water react with CO ₂ to produce bicarbonate bicarbonate (RNH ₂ + H ₂ O + CO ₂ ⇔ RNH ₃ ⁺ + HCO ₃ ⁻ ). Absorption / desorption can be performed with the lowest energy reaction (bicarbonate-carbonate). All amine systems require gas-liquid contactors and strippers. The system described here is preferred in that it is a very efficient gas-liquid contactor. While any amine system has advantages, the carbonate / ammonium bicarbonate sorbent was chosen because ammonia is cheaper and the reaction energy of ammonia is lower than alkanolamines such as MEA.

Alkali carbonates include Na, K, and Ca, carbonate / bicarbonate. Alkali carbonates were used heavily in the early 1900s for the purpose of ambient temperature and CO ₂ pressure absorption, but have recently been replaced by more efficient alkanolamines. Since the absorption rate of CO _{2 into} an aqueous solution is usually slow, an accelerator (catalyst or enzyme) is often added to increase the rate.

Examples of promoters include formaldehyde, MEA, DEA, glycine, and carbonic anhydrase as described by Kohl et al., “Gas Purification”, Gulf Professional Publishing, Fifth Edition, 1997, incorporated herein by reference. . The fastest catalyst available for CO ₂ absorption is an enzyme called carbonic anhydrase (MC Trachenberg, L Bao, SL Goldman et al., 2004, 7th International Conference on Greenhouse Gas Control Technology (GHGT), incorporated herein by reference. -7), see Bankover, BC). Amino acids are also used as promoters of absorption of CO ₂ equivalent to or exceeding MEA or DEA as described in Jacco van Holst, Patricia. P. Politiek, John P. M.M. Niederer, Geert F .; Versteeg et al., Eighth International Conference on Greenhouse Gas Control Technology, 2006, “CO ₂ capture from flue gas using amino acid salt solution”, which is incorporated herein by reference. Enzymes and catalysts do not change the reaction energy or change its equilibrium point, but lower the activation energy and increase the reaction rate on the order of a few magnitudes. Hydrolysis of CO ₂ in water 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 a pressure fluctuation process must be used. Since the partial pressure of CO ₂ in the combustion exhaust gas is about 0.15 atm, when capturing pure CO ₂ , the total desorption pressure needs to be less than about 0.1 atm. As another CA candidate, there is a method of pressurizing all combustion exhaust gas before contact. Other accelerators (such as DEA) are currently utilized in hot potassium carbonate processes performed at high temperatures and pressures.

The hybrid sorbent utilizes a combination of carbonate and sorbent sand carbonate with an amine. An example currently used is K ₂ CO ₃ / PZ, which is an aqueous potassium carbonate solution in which piperazine (PZ), which is expected to use less energy than MEA, is used as an accelerator. This system is currently being studied at the University of Texas at Austin. The absorption rate and load of CO ₂ is significantly greater for K ₂ CO ₃ / PZ than for MEA. In addition, the loss and degradation of PZ is much less than that of MEA, according to Plasyski et al. “Capacity capture by carbon dioxide, carbon sequestration, full picture of project”, USDOE, NETL, April (2008). As described in. The major contribution of GLC absorbers 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 described chemical absorption / desorption system is pH variation, which is usually not mentioned due to the very high energy costs. CO ₂ is absorbed with NaOH resembling a base and released with HCl resembling an acid. The resulting salt is electrolyzed to regenerate the acid and base. Energy input is utilized electrochemically, not pressure or temperature fluctuations. The calculated energy requirements are much higher than those of other processes. But this process is commercialized in SO ₂ absorption applications. Physical sorbents include glycols, metal organic frameworks (MOFs), ionic liquids, seawater, and underground brines. These utilize physical absorption rather than chemical reaction with sorbent. Although chemical reactions do not involve energy, desorption processes require pressure changes.

Glycols work best at the high temperatures utilized in pressure fluctuation processes (such as Celexsol process) that have been proposed as a process to separate CO ₂ before combustion with 700 psi synthesis gas. Gas-liquid contact systems are not available for high pressure absorption processes.

The metal organic framework (MOF) is a “cage” of molecules that contain small bubbles of CO ₂ gas. MOF is very selective, has excellent absorption / desorption rates, has a high CO ₂ capacity, and can be used for gas-liquid contactors and liquid membranes. However, the high reagent cost and the fact that it has not been used in gas-liquid contactors are risks.

An ionic liquid is an organic salt that is liquid at room temperature, not an aqueous solution. Since ionic liquid absorbs both CO ₂ and SO ₂ , it is highly expected for combustion exhaust gas cleaning. It can be used for gas-liquid contactors and liquid films. Similar to MOF, ionic liquids can be synthesized on a laboratory scale only, and reagent costs can be very high. Furthermore, no tests with gas-liquid contactors have been performed.

For underground brine or seawater, the preferred method for CO ₂ sequestration is injection into a deep saline aquifer, so a potential method for both capture and sequestration is to convert CO ₂ to natural alkaline It is absorbed with underground brine and injected again into the solution. Thus, the energy at the time of compression to desorb the CO ₂ to be injected as a gas is not necessary. Depending on the alkalinity of the groundwater, the absorption rate may be delayed and a large contact area may be required. A very large surface area of the GLC contactor is a perfect solution. In addition, even though many naturally occurring aquifers are rich in Ca and / Mg, groundwater alkalinity may need to be enhanced by lime, providing optimal capital and operating costs. Trade-off relationships need to be taken into account.

This process is similar to seawater absorption of either / both CO ₂ or SO ₂ , with essentially unlimited absorption and disposal (depending on the site of course). In addition, seawater is naturally rich in Ca and Mg that can readily form solid precipitates as carbonates or sulfates. This or other desired ratio can also be artificially generated utilizing various magnesium and / or calcium salts such as nitrates, hydroxides, sulfates, carbonates, or halides. Since the solubility of these salts varies dramatically depending on the starting compound, pH, and temperature of the target solution, those skilled in the art need to take into account their own purpose and the compound of interest.

The following table compares the advantages, disadvantages, and estimated costs between the various CO ₂ sorbent systems available for gas-liquid contactors.

It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the scope or spirit of the invention. Thus, it is intended that the present invention include modifications and variations of this invention that come within the scope of the following claims and their equivalents.
(Item 1)
A liquid inlet;
A gas inlet;
A gas outlet;
A nozzle array that communicates with the liquid inlet and the gas inlet to generate a plurality of uniformly spaced flat liquid jets having a shape that minimizes disturbance from the gas;
A gas-liquid separator that allows liquid to pass while substantially preventing gas from passing;
A liquid outlet in fluid communication with the gas-liquid separator;
A gas-liquid contact module comprising:
(Item 2)
The module according to item 1, further comprising at least two gas-liquid contact modules connected in parallel.
(Item 3)
The module according to item 1, further comprising at least two gas-liquid contact modules connected in series.
(Item 4)
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, coated metal, and combinations thereof.
(Item 5)
The module according to Item 1, wherein the gas-liquid contact module includes a plastic material.
(Item 6)
The module according to Item 1, wherein the gas-liquid contact module includes at least one of a structural polymer, polyimide, a composite thereof, and a combination thereof.
(Item 7)
The module according to item 1, wherein the nozzle array includes a plurality of nozzles in a staggered configuration.
(Item 8)
The module according to item 1, wherein the gas-liquid contact module has a size for processing an increment of an entire predetermined processing requirement.
(Item 9)
The module of item 1, wherein the nozzle array is oriented to provide a cross-flow gas-liquid contact module.
(Item 10)
The module of item 1, wherein the nozzle array is oriented to provide a co-current gas-liquid contact module.
(Item 11)
The module of item 1, wherein the nozzle array is oriented to provide a reverse flow gas-liquid contact module.
(Item 12)
The module of item 1, wherein the nozzle array includes at least two nozzles separated by a distance greater than about 0.2 cm.
(Item 13)
Item 2. The module of item 1, wherein the nozzle array includes at least one row of nozzles.
(Item 14)
Item 2. The module of item 1, wherein the nozzle array comprises at least three rows of nozzles separated by a uniform distance.
(Item 15)
The module of item 1, wherein the nozzle array includes a U-shaped channel.
(Item 16)
The module according to item 1, wherein the nozzle array includes a V-shaped channel.
(Item 17)
The module of item 1, wherein the nozzle array includes channels having a depth greater than about 2 mm.
(Item 18)
The module of item 1, wherein the nozzle array includes channels having a depth in the range of about 2 mm to about 20 mm.
(Item 19)
The module of item 1, wherein the liquid inlet supplies liquid to the nozzle array at an angle of about 90 degrees to the nozzle channel.
(Item 20)
The nozzle array includes a first row of nozzles, a second row of nozzles, and a third row of nozzles, wherein the second row of nozzles includes the first row of nozzles and the third row of nozzles. The module according to item 1, wherein the second row nozzles are offset from the first row nozzles and the third row nozzles.
(Item 21)
The module according to item 1, wherein the nozzle array includes at least one nozzle having a ratio of a minor axis to a major axis of less than 0.5.
(Item 22)
The module of item 1, wherein the nozzle array includes at least one nozzle having a projected cross-sectional area in the range of about 0.25 mm ² to about 20 mm ² .
(Item 23)
A module according to item 1, wherein the gas-liquid separator substantially minimizes back splash of liquid during operation.
(Item 24)
The module according to Item 1, wherein the gas-liquid separator includes a plurality of components.
(Item 25)
25. The module of item 24, wherein the plurality of components includes a plurality of curved vane pumps spaced from each other.
(Item 26)
25. The module of item 24, wherein the plurality of components includes a plurality of angled vane pumps spaced from one another.
(Item 27)
Item 2. The module according to Item 1, further comprising a liquid drain plenum provided adjacent to the gas-liquid separator.
(Item 28)
28. The module according to item 27, further comprising a demister that removes at least a part of the liquid mixed in the gas.
(Item 29)
29. The module of item 28, wherein the demister includes a plurality of baffles.
(Item 30)
29. The module according to item 28, wherein the demister is provided adjacent to the gas outlet.
(Item 31)
The module according to item 1, wherein the liquid flat jet includes at least one of water, ammonia, ammonia salt, amine, alkanolamine, alkali salt, alkaline earth salt, peroxide, and hypochlorite.
(Item 32)
The module according to Item 1, wherein the liquid flat jet includes at least one of an aqueous calcium salt solution and an aqueous magnesium salt solution.
(Item 33)
The module according to Item 1, wherein the liquid flat jet includes seawater.
(Item 34)
A module according to item 1, wherein the liquid inlet contains salt water.
(Item 35)
A method of treating gas phase molecules with a gas-liquid contactor,
Forming a plurality of essentially planar liquid jets, each comprising a planar liquid sheet, each configured on a substantially parallel plane;
Providing a gas comprising at least one reactive or soluble gas phase molecule;
Removing at least some of the gas phase molecules by interaction by mass transfer between the gas phase molecules and the plurality of liquid jets;
A method comprising:
(Item 36)
36. The method of item 35, wherein the mass transfer interaction has a volume mass transfer coefficient in the range of about 1 sec- ¹ to about 250 sec- ¹ .
(Item 37)
36. The method of item 35, wherein the mass transfer interaction has a volume mass transfer coefficient in the range of about 5 sec- ¹ to about 150 sec- ¹ .
(Item 38)
36. The method of item 35, wherein the mass transfer interaction has a volumetric mass transfer coefficient in the range of about 10 sec- ¹ to about 100 sec- ¹ .
(Item 39)
The step of supplying the gas includes:
36. The method of item 35, comprising providing a gas wherein the ratio of the gas flow rate to the reaction chamber volume ranges from about 100 min- ¹ to about 1000 min- ¹ .
(Item 40)
Forming an array of the plurality of flat liquid jets having uniform spacing;
36. The method of item 35, comprising forming the flat liquid jet at a hydraulic pressure in the range of about 2 psig to about 50 psig.
(Item 41)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a width greater than about 1 cm.
(Item 42)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a width in the range of about 1 cm to about 15 cm.
(Item 43)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a thickness in the range of about 10 μm to about 1000 μm.
(Item 44)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a thickness in the range of about 10 μm to about 250 μm.
(Item 45)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a thickness in the range of about 10 μm to about 100 μm.
(Item 46)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a length in the range of about 5 cm to about 30 cm.
(Item 47)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a length in the range of about 5 cm to about 20 cm.
(Item 48)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a velocity of less than 15 m / sec.
(Item 49)
36. The method of item 35, wherein at least one of the plurality of flat liquid jets of the array has a velocity in the range of about 5 m / sec to about 15 m / sec.
(Item 50)
A method for removing gas phase molecules with the apparatus of item 1.
(Item 51)
51. The method according to Item 50, wherein the gas phase molecule includes at least one of sulfur oxide, nitrogen oxide, carbon dioxide, ammonia, acid gas, amine, halogen, and oxygen.
(Item 52)
51. A method according to item 50, wherein the gas phase molecules include sulfur oxides.
(Item 53)
51. A method according to item 50, wherein the gas phase molecules include carbon dioxide.
(Item 54)
51. A method according to item 50, wherein the gas phase molecules include nitrogen oxides.
(Item 55)
51. The method of item 50, wherein the gas phase molecule comprises an amine.
(Item 56)
51. A method according to item 50, wherein the gas phase molecules include chlorine.
(Item 57)
The planar plurality of liquid jets may include at least one of water, ammonia, ammonia salt, amine, alkanolamine, alkali salt, alkaline earth salt, peroxide, and hypochlorite. The method described.
(Item 58)
36. A method according to item 35, wherein the plurality of planar liquid jets include at least one of an aqueous calcium salt solution and an aqueous magnesium salt solution.
(Item 59)
36. A method according to item 35, wherein the planar plurality of liquid jets includes seawater.
(Item 60)
36. A method according to item 35, wherein the plurality of planar liquid jets includes salt water.
(Item 61)
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 coupled to the liquid plenum, each including a planar liquid sheet and providing a plurality of essentially planar liquid jets each configured on a substantially parallel plane;
A gaseous fluid separator coupled to the reaction chamber;
Gas-liquid contact system comprising.
(Item 62)
64. The system of item 61, further comprising a secondary chemical processing subsystem in fluid contact with the liquid plenum.
(Item 63)
62. The subsystem according to item 61, wherein the gas-liquid contact system mineralizes the absorbed sulfur oxide into a sulfite or a sulfate.
(Item 64)
62. The subsystem according to Item 61, wherein the gas-liquid contact system mineralizes absorbed CO ₂ into carbonate.
(Item 65)
Subsystem of claim 61 the gas-liquid contact system, which releases pure CO ₂ for tertiary treatment.
(Item 66)
Item 63. The subsystem according to Item 61, wherein the gas-liquid contact system reacts the absorbed nitrogen oxides into a soluble nitrate.
(Item 67)
62. The system according to Item 61, further comprising a demister provided at the gas outlet.
(Item 68)
68. The system of item 67, further comprising a gas outlet plenum coupled to the gas outlet.
(Item 69)
The system of item 68, further comprising a capture tank in fluid communication with the reaction chamber.
(Item 70)
62. A system according to item 61, wherein the nozzle array includes a plurality of nozzles in a staggered configuration.
(Item 71)
62. A system according to item 61, wherein the nozzle array is oriented to provide a cross-flow gas-liquid contact system.
(Item 72)
62. A system according to item 61, wherein the nozzle array is oriented to provide a co-current gas-liquid contact system.
(Item 73)
62. A system according to item 61, wherein the nozzle array is oriented to provide a back-flow gas-liquid contact system.
(Item 74)
62. A system according to item 61, wherein the nozzle array includes at least one row of nozzles.
(Item 75)
62. A system according to item 61, wherein the nozzle array includes a U-shaped channel.
(Item 76)
62. A system according to item 61, wherein the nozzle array includes a V-shaped channel.
(Item 77)
64. The system of item 61, wherein the nozzle array includes channels having a depth greater than about 2 mm.
(Item 78)
64. 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.
(Item 79)
64. The system of item 61, wherein the nozzle array includes at least one nozzle having a minor axis to major axis ratio of less than 0.5.
(Item 80)
62. The system of item 61, wherein the nozzle array includes at least one nozzle having a projected cross-sectional area in the range of about 0.25 mm ² to about 20 mm ² .
(Item 81)
A gas-liquid contactor,
A fluid plenum for supplying contact liquid;
A contact chamber in communication with the fluid plenum for receiving the contact liquid from the fluid plenum;
A gas inlet in communication with the contact chamber;
A gas outlet in communication with the contact chamber;
With
The gas-liquid contactor system is a gas-liquid contactor that interacts by mass transfer having a volumetric mass transfer coefficient in the range of about 5 sec- ¹ to about 250 sec- ¹ .
(Item 82)
82. The gas-liquid contactor according to item 81, further comprising a nozzle array.
(Item 83)
82. A gas-liquid contactor according to item 81, wherein the nozzle array includes at least one row of nozzles.
(Item 84)
82. A gas-liquid contactor according to item 81, wherein the nozzle array includes a U-shaped channel.
(Item 85)
82. The gas-liquid contactor according to item 81, wherein the nozzle array includes a V-shaped channel.
(Item 86)
84. The gas-liquid contactor of item 81, wherein the nozzle array includes a channel having a depth greater than about 2 mm.
(Item 87)
82. A gas-liquid contactor according to item 81, wherein the volume mass transfer coefficient is in the range of about 10 seconds- ¹ to about 100 seconds- ¹ .
(Item 88)
82. A gas-liquid contactor according to item 81, wherein the volume mass transfer coefficient is in the range of about 5 seconds- ¹ to about 25 seconds- ¹ .
(Item 89)
A gas phase molecular processing system comprising a plurality of modular gas-liquid contactors arranged in parallel or in series so as to be sized according to gas phase molecular processing.
(Item 90)
90. Each of the plurality of modular gas-liquid contactors includes a nozzle array that provides a plurality of basically planar liquid jets, each of the plurality of liquid jets including a planar liquid sheet. System.
(Item 91)
51. A method according to item 50, wherein the gas phase molecule comprises a volatile organic compound.

Claims (27)

A gas-liquid contact module configured to be arranged in parallel or in series with another gas-liquid contact module,
A liquid inlet;
A nozzle array that passing the liquid inlet and communicating,
A contact chamber for receiving the liquid from the liquid inlet via the nozzle array;
A gas inlet in communication with the contact chamber and supplying gas to the contact chamber;
A gas outlet that communicates with the contact chamber and conveys the gas from the contact chamber to the outside; a liquid collection chamber that is disposed at a lower portion of the contact chamber and collects a liquid that forms a plurality of planar liquid jets;
Gas-liquid separation disposed between the contact chamber and the liquid collection chamber and having a hole through which the plurality of planar liquid jets pass and separates the plurality of planar liquid jets from the gas flow And
With
The nozzle array is configured to generate the plurality of planar liquid jets substantially parallel to the gas flow;
The nozzle array is
A nozzle plate disposed at the top of the contact chamber ;
At least one nozzle row removably disposed on the nozzle plate;
Have
Each of the at least one nozzle row includes a plurality of nozzles arranged in a straight line,
Each of the plurality of linearly arranged nozzles is configured to generate one of the plurality of planar liquid jets;
Gas-liquid contact module. Wherein each of the plurality of nozzles of the at least one nozzle row, the liquid inlet communicating with a U-type, was V-type or a orifice formed in the liquid channel of semicircular,
The liquid channel has a depth of 2 mm or more;
The gas-liquid contact module according to claim 1. Wherein the plurality of nozzles of the at least one nozzle row, viewed contains an orifice of oblong shape,
The ratio of the minor axis to the major axis of the elliptical orifice is less than 0.5;
The gas-liquid contact module according to claim 1 or 2. The projected area of the orifice opening is in the range of 0.25 mm ² to 20 mm ² .
The gas-liquid contact module according to claim 2 or claim 3 . The plurality of nozzles of the at least one nozzle row includes at least two nozzles separated by a distance greater than 0.2 cm;
The gas-liquid contact module according to any one of claims 1 to 4. The at least one nozzle row includes at least two nozzle rows arranged in a staggered configuration;
The gas-liquid contact module according to any one of claims 1 to 5 . The nozzle array includes the plurality of gas flows substantially parallel to the gas flow such that the gas flow is a cross flow, a parallel flow or a counter flow with respect to the liquid flow of the plurality of planar liquid jets . Producing a planar liquid jet,
The gas-liquid contact module according to any one of claims 1 to 6 . The liquid inlet supplies liquid to the nozzle array at an angle of 90 degrees to the nozzle channel;
The gas-liquid contact module according to any one of claims 1 to 7 . The gas-liquid separator suppresses back splash of the plurality of planar liquid jets;
The gas-liquid contact module according to any one of claims 1 to 8 . The gas-liquid contact module includes at least one material selected from the group consisting of copper, nickel, chromium, steel, aluminum, coated metal, plastic material, and polyimide,
The gas-liquid contact module according to any one of claims 1 to 9 . The plurality of planar liquid jets include at least one of water, ammonia, ammonia salts, amines, alkanolamines, alkali salts, alkaline earth salts, peroxides, and hypochlorites.
The gas-liquid contact module according to any one of claims 1 to 10 . A liquid outlet that communicates with the liquid collection chamber and allows the liquid to flow out of the gas-liquid contact module;
A pump connected to the liquid outlet for circulating the liquid collected in the liquid collection chamber to the liquid inlet;
Further comprising
The gas-liquid contact module according to any one of claims 1 to 11 . A demister that is disposed between the contact chamber and the gas outlet and removes at least a part of the liquid mixed in the gas;
The gas-liquid contact module according to any one of claims 1 to 12 . At the end of the nozzle plate , a groove configured to fit into a pin attached to the frame of the gas-liquid contact module is formed,
The groove is formed such that when the pin is fitted into the groove, an elastomer seal that seals the nozzle plate against the surface of the frame is pressurized.
The gas-liquid contact module according to any one of claims 1 to 13 . Using the gas-liquid contact module according to any one of claims 1 to 14 ,
A method of removing gas phase molecules contained in the gas and having reactivity or solubility with respect to the liquid. The gas phase molecule includes at least one of sulfur oxide, nitrogen oxide, carbon dioxide, ammonia, acid gas, amine, halogen, and oxygen.
The method of claim 15 . Forming the plurality of planar liquid jets;
Supplying the gas containing the gas phase molecules;
Removing at least a portion of the gas phase molecules by mass transfer interaction between the gas phase molecules and the plurality of planar liquid jets;
including,
17. A method according to claim 15 or claim 16 . The mass transfer interaction has a volume mass transfer coefficient in the range of 1 sec ⁻¹ to 250 sec ⁻¹ ;
The method of claim 17 . Forming the array of the plurality of planar liquid jets having uniform spacing comprises:
Forming the plurality of planar liquid jets at a hydraulic pressure in the range of 13.79 kPa (2 psi) to 344.75 kPa (50 psi);
19. A method according to claim 17 or claim 18 . Supplying the gas comprises:
Providing a gas whose ratio of gas flow rate to reaction chamber volume ranges from 100 min- ¹ to 1000 min- ¹ .
The method according to any one of claims 17 to claim 19. A plurality of gas-liquid contact modules according to any one of claims 1 to 14 ,
Gas-liquid contact system. Including at least two gas-liquid contact modules connected in parallel or in series;
The gas-liquid contact system according to claim 21 . The gas-liquid contact system mineralizes absorbed sulfur oxides into sulfites or sulfates, mineralizes absorbed CO ₂ into carbonates, or reacts absorbed nitrogen oxides to form soluble nitrates. To
The gas-liquid contact system according to claim 21 or claim 22 . A secondary chemical processing subsystem in communication with the gas-liquid contact module;
The gas-liquid contact system according to any one of claims 21 to 23 . In at least one of the plurality of gas-liquid contact modules, CO ₂ contained in the gas is absorbed by the liquid,
The gas-liquid contact system includes:
From the liquid that has absorbed the CO _2, further comprising a CO ₂ stripper to release CO _2,
The gas-liquid contact system according to any one of claims 21 to 24 . The gas-liquid contact system includes:
Removing at least a portion of the gas phase molecules from the gas by an interaction by mass transfer between the gas phase molecules contained in the gas and the plurality of planar liquid jets;
The mass transfer interaction has a volumetric mass transfer coefficient in the range of 5 sec- ¹ to 250 sec- ¹ .
The gas-liquid contact system according to any one of claims 21 to 25 . Including a first gas-liquid contact module and a second gas-liquid contact module;
A gas containing an acid gas is supplied to the gas inlet of the first gas-liquid contact module,
The liquid inlet of the first gas-liquid contact module is supplied with a liquid containing ammonia and having a pH higher than 7.
Gas discharged from the gas outlet of the first gas-liquid contact module is supplied to the gas inlet of the second gas-liquid contact module,
A liquid adjusted to conditions suitable for capturing ammonia is supplied to the liquid inlet of the second gas-liquid contact module;
The gas-liquid contact system according to any one of claims 21 to 26 .

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