JP7281354B2 - Emission control system and method of controlling emissions - Google Patents

Description

CROSS REFERENCE TO RELATED APPLICATIONS This application claims priority to U.S. Provisional Application No. 62/029,044 filed July 25, 2014 and U.S. Provisional Application No. 62/133,791 filed March 16, 2015. No. 15/606,704, filed May 26, 2017, which is a continuation-in-part of U.S. Patent Application No. 14/808,563, filed July 24, 2017. The entire disclosure of the above application is incorporated herein by reference.

The present disclosure relates generally to industrial emission control systems and methods, and devices used in such systems, and methods of removing pollutants from gaseous and non-gaseous emissions.

This section presents background information related to the present disclosure that is not necessarily prior art.

Industries in many economic sectors produce more than one type of emissions. Such emissions can be divided into two basic groups, one gaseous and the other non-gaseous. Emissions in the gas group and non-gas group emissions often contain hazardous pollutants. Emissions in the gas group may be exhaust gases generated by coal-fired plants or natural gas-fired installations. Effluents in the non-gas group may be liquid, sludge-like or slurry-like materials. Neutralize, capture, collect, remove, dispose of, and/or provide some sort of It must be properly sealed by means.

Many industries rely on burning fuels as a means to accomplish some aspect of their respective methods. For example, as a first example, steel mills burn and/or melt metal during metal forming, extrusion and other metal casting processes. Methods used within this metal industry involve operations that release powders as metal vapors and ionized metals. Pollutants harmful to the environment, plants, animals and/or humans are released into the air via metal vapors. To a greater or lesser extent, hazardous contaminants in this metal vapor and/or metal vapor compounds must be collected and properly disposed of. As a second example, mining operations for precious metals such as gold, silver and platinum also generate metals, metal vapor emissions and powders containing heavy metal contaminants, which must be captured, collected and properly disposed of. If not, it is considered harmful. As a third example, industries that burn natural gas produce effluents that often contain high levels of pollutants, which are considered hazardous if not captured, collected and properly disposed of. As a fourth example, an energy producer that uses coal as a combustible consumable to produce steam in boilers that rotate electrical generators may produce metal vapors and metal compounds that are considered dangerous to the environment, plants, animals and humans. Generates significant amounts of emissions containing Among other harmful pollutants, metal vapor emissions often contain mercury (Hg).

Because of the global jet stream pattern, airborne metal vapor emissions can be transported from one country and deposited in another. For example, much of the mercury emissions originating in China and/or India may actually end up in ocean waters in and/or between the United States. Similarly, much of the mercury-bearing emissions generated in the United States may actually be deposited in the oceans of Europe and/or in between. Completing this cycle, mercury-bearing emissions originating in Europe may actually deposit in China and/or India. Mercury and other toxic pollutants in effluents from industrial processes are therefore a global problem of global significance that requires global efforts to be resolved.

National and international regulations, rules, limits, fees, oversight, and many more stringent laws, pending revision, have been proposed and/or implemented against those that generate such emissions. For example, one of the most harmful and regulated contaminants in metal vapor emissions is mercury. Human-industrial processes have increased the accumulation of mercury and/or mercury deposits far beyond naturally occurring levels. At the global level, the total amount of mercury released by human activities is estimated to be 1960 metric tons per year. This figure was calculated from data analyzed in 2010. Globally, the largest contributors to this particular type of emissions are coal burning (24%) and gold mining (37%) activities. In the United States, coal burning accounts for a higher proportion of emissions than gold mining activities.

For animals and humans, the major problem with exposure to mercury is that mercury is a bioaccumulator. Therefore, any amount of mercury ingested by a fish or other animal remains (i.e. accumulates) in that animal and is transferred to humans or, if the former is ingested by the latter, to other animals. . Furthermore, mercury is not excreted from the body of the ingesting host. Larger predators that live the longest and/or prey on large numbers of other animals in the food chain are most at risk of excess mercury accumulation. Humans who eat mercury-containing animals (particularly fish) are exposed to a wide range of well-known medical problems, including neurological disorders and/or reproductive problems.

There are three main types of mercury emissions: Anthropogenic releases, re-releases and natural releases. Anthropogenic releases are largely the product of industrial activity. Anthropogenic sources include industrial coal burning plants, natural gas burning plants, cement production plants, petroleum refineries, chlor-alkali industries, vinyl chloride industries, mining operations and refining operations. Re-release occurs when soil-deposited mercury is redistributed by floods or forest fires. Mercury absorbed and/or deposited in soil is released back into the water by storm runoff and/or flooding. Soil erosion contributes to this problem. Forest fires, whether natural, arson, or deliberate deforestation fires, re-release mercury into the air and/or water sources, and deposit it elsewhere. Natural emissions include volcanoes and geothermal vents. Approximately half of all mercury released into the atmosphere is estimated to come from natural events such as volcanoes and geothermal vents.

As noted above, coal-burning plants release large amounts of mercury and other pollutants into the environment each year. Accordingly, numerous efforts are currently underway to reduce the amount of harmful pollutants in flue gas emissions generated by coal-fired plants. Many coal-fired plants in the United States are equipped with emission control systems that capture, contain, and/or regenerate hazardous elements such as mercury. In a coal-fired plant, coal is burned to boil water, convert water to steam, and drive a generator. Flue gas emissions from coal combustion are often sent through a conduit system to a fluid gas desulfurization unit and/or an injection dryer system to remove some emissions from the flue gas and sulfur dioxide (SO2 ) and hydrogen chloride (HCl) are removed. A conventional conduit system then directs the flue gas stream to a wet/dry scrubber where more sulfur dioxide, hydrogen chloride and fly ash are removed. The flue gas stream is passed through a baghouse where particles are separated from the air stream in the flue gas, similar to a domestic vacuum cleaner bag. The flue gas passes through a filter-like bag having a porosity that allows air flow but impermeable to larger particles moving in the air flow. The surface of the filter bag is agitated and/or washed to collect the trapped particles and make them ready for disposal. Generally, these deposits are themselves hazardous emissions and must be disposed of. The remainder of the flue gas that has passed through this type of emission control system passes through a tall chimney and is discharged to the atmosphere.

A problem with this type of emission control system is that it is not practically effective at capturing and/or collecting heavy metals such as mercury contained in metal vapors and vaporous metal compounds. Because coal-fired systems burn coal at relatively high temperatures, approximately 1500 degrees Fahrenheit, mercury turns into nano-sized particles that can pass through even the most efficient filter systems. As a result, large amounts of airborne mercury and other harmful pollutants are released into the atmosphere.

Several known systems have been developed to meet this challenge to capture and collect mercury from coal combustion systems and/or other sources of emissions. These fall into one of three categories.

The first category is a group of methods and/or systems that capture mercury by injecting sorbents into the flue gas stream. Besides precious metals, the most common sorbent materials are activated carbon and/or biochar. Activated carbon is often halogenated with bromine. Biochar is carbon-rich charcoal. Injecting the sorbent into the flue gas facilitates the capture of pollutants in one and/or combination of the following conventional emission control devices. An electrostatic precipitator, a fluidized gas desulfurization system, a washer system, or a fiber filter system. There are several variations of these systems that require injecting activated carbon at various points in the emissions control system after coal combustion. Some exemplary methods and/or systems in the first category are disclosed in U.S. Pat. 7,704,920, 7,141,091, 6,905,534, 6,712,878, 6,695,894, 6,558,454, 6,451,094, 6,136,072, 7, 618,603, 7,494,632, 8,747,676, 8,241,398, 8,728,974, 8,728,217, 8,721,777, 8,685,351, and 8,029 , 600.

The second category is methods and/or systems for pre-treating coal fuel prior to combustion to reduce mercury levels in coal fuel. Some exemplary methods and/or systems in this second category are described in U.S. Pat. All of the methods and/or systems described in these exemplary patents produce large amounts of unusable coal, which is also considered hazardous waste. As a result, methods and/or systems of the second category of known solutions are inefficient and expensive to implement. Furthermore, coal pretreatment often requires large amounts of capital and physical space, making it impractical to retrofit many existing emission control systems with the necessary equipment.

The third category is a group of methods and/or systems that inject catalyst into emissions control equipment upstream of the activated carbon injection system. The catalysts in these methods and/or systems ionize mercury to facilitate its collection and removal from flue gases. However, the efficiency of such methods and/or systems is low, leading to high operating costs, and methods and/or systems of the third category of this known solution are not cost effective. Examples of this third category are described in US Pat. In addition to these examples, US Pat. No. 7,214,254 discloses a method and apparatus for regenerating expensive adsorbent materials using microwaves and fluidized bed reactors. This method selectively evaporates mercury from the sorbent, at which point it can be captured by special filters or concentrated for collection. Due to the use of microwaves, this method is not practical for large-scale commercial applications and is therefore only useful for regenerating expensive adsorbents. U.S. Patent Application No. 2006/0120935 describes another method of removing mercury from flue gas by using one of several substrate materials to impart an affinity to mercury as the flue gas passes through an emissions control facility. Disclose an example. This method is also impractical for large-scale commercial use. Accordingly, current emission control systems and methods generally operate by moving hazardous pollutants from gaseous emissions to non-gaseous emissions, thereby creating additional emissions management problems.

While many laws and regulations focus on metal vapor emissions, slurry and/or slurry emissions, sludge and/or sludge emissions, liquid and/or liquid emissions, and other types of emissions. Effluents containing other forms of hazardous pollutants, such as, should not be overlooked. All types of effluents listed also require treatment to neutralize, capture, collect, remove, dispose of, and/or appropriately seal in some way the hazardous contaminants they contain. there's a possibility that. Historically, the most cost-effective and most widely used hazardous pollutant removal process has employed activated carbon (in some form) through which the effluent passes. Accordingly, the demand for activated carbon in the United States is projected to exceed £1 billion annually and grow annually through 2017, costing industry in excess of $1 to $1.50/lb. This equates to approximately $1 billion annually. Much of the projected increase in activated carbon demand will be influenced by the implementation of regulations promulgated by the EPA requiring utilities and manufacturers to update their coal-fired plants to comply with stricter requirements.

In addition to stricter gas emissions regulations, the EPA has also added stricter regulations on non-gaseous emissions through the Clean Water Act, which must be fully compliant by 2016. Composite regulations tightened for all types of emissions cover multiple types of emissions produced by a variety of different industries. Utilities that burn fuel to produce electricity, such as power utilities, generate primary gaseous emissions that contain hazardous pollutants. In accordance with industry standards, these gaseous effluents are exposed to activated charcoal to capture sufficient quantities of noxious contaminants to bring the contaminants of the gaseous effluents to below acceptable limits. The process of removing hazardous pollutants from the gaseous emissions produced by burning this fuel produces secondary non-gaseous emissions, which are liquid or slurry materials containing hazardous pollutants. Hazardous pollutants in this secondary non-gaseous effluent must also be captured and/or appropriately sealed to prevent release of this hazardous pollutant into the environment. Both primary gaseous emissions and secondary non-gaseous emissions require means to adequately capture and/or regenerate and/or contain sufficient hazardous pollutants to comply with environmental standards. and The industrial costs of known methods capable of removing hazardous pollutants from secondary non-gaseous emissions are almost prohibitive, and some industries are forced to invest in equipment if the costs cannot be added to the consumer. forced to close.

According to some practices, non-gaseous effluents that are considered hazardous because they contain high levels of contaminants are disposed of and stored in ponds, piles or dry beds for long periods of time. While such practices isolate hazardous pollutants, they are costly and consume land without neutralizing the hazardous pollutants themselves, which can lead to environmental problems at the camp. have a nature. One example of non-gaseous emissions is fly ash, which is a natural product of burning coal. Fly ash is essentially identical in composition to volcanic ash. Fly ash contains trace concentrations (i.e., trace amounts) of many types of heavy metals and other known harmful and toxic contaminants (e.g., mercury, beryllium, cadmium, barium, chromium, copper, lead, molybdenum, nickel, radium, selenium, thorium, uranium, vanadium, zinc). By one estimate, 10% of the coal burned in the United States consists of non-combustible material, which becomes ash. Therefore, the concentration of harmful trace elements in coal ash is ten times higher than the concentration of these elements in the original coal.

Fly ash is considered a pozzolanic material and, when mixed with calcium carbonate, forms a cementitious material that agglomerates with water and other compounds to produce concrete mixtures suitable for roads, airport runways and bridges. has long been used in the production of Fly ash produced in coal-fired plants is flue ash consisting of ultra-fine particles that rise with the flue gas. Ash that does not rise is often called bottom ash. Early coal-fired plants simply released fly ash into the atmosphere. In recent years, environmental regulations have created a need to install emission control mechanisms to prevent fly ash from being released into the atmosphere. Many plants use electrostatic precipitators to trap fly ash before it reaches the chimney and escapes to the atmosphere. Bottom ash is usually mixed with captured fly ash to form what is known as coal ash. Fly ash typically contains higher levels of toxic contaminants than bottom ash, whereby mixing bottom ash and fly ash produces a proportionate level of toxic pollution that complies with many standards for non-gaseous emissions. Substance is produced. However, future standards may redefine fly ash as a hazardous material. If fly ash is redefined as a hazardous material, it will no longer be available for use in cement, asphalt manufacturing and other widely used applications. According to one study, a ban on fly ash use in concrete manufacturing would increase costs by more than $5 billion per year in the United States alone. This cost increase is a direct result of replacing fly ash with another, more expensive material. In addition, due to its unique physical properties, there are no other known suitable direct replacements for fly ash as a cement additive.

More than 130 million tons of fly ash are produced annually in more than 450 coal-fired power plants in the United States, according to the report. One report estimates that only 40% of fly ash is recycled, which is 52 million tons/year of fly ash recycled, while 78 million tons/year remain in slurry ponds and mountains. Indicates that it is reserved. Fly ash is typically stored in wet slurry ponds to reduce entrainment of airborne particles and contaminants out of bulk reservoirs into the atmosphere or surrounding environment. In addition to the airborne release of bulk stored fly ash, there is also the risk of damage and/or failure of the containment systems necessary to contain fly ash for extended periods of time. In a notorious 2008 failure in Tennessee, the levee of a wet fly ash reservoir collapsed, spilling 5.4 million cubic yards of fly ash. This overflow of fly ash destroyed several homes and polluted nearby rivers. Cleaning costs are undetermined at the time of filing this application and may exceed $1.2 billion.

As another example, non-gaseous emissions may be found as a by-product of the wastewater generation system of conventional coal-fired plants. A typical wastewater generation system produces large amounts of water from boilers and water cooling processes. These bulk wastewaters contain relatively low levels of contaminants and are used to dilute other wastewater streams containing higher levels of contaminants. The contaminated wastewater stream, which is normally discharged from the scrubber, is diluted with bulk wastewater from the boiler and/or cooling water process and then treated with lime in a large continuous mixing tank to form gypsum and then It is pumped to the sedimentation pond. During this process, certain amounts of mercury and other heavy metals are incorporated into the gypsum and stabilized for use in wallboard and cement. This gypsum is generally considered non-leaching and is not considered a contamination. However, the water from the sedimentation basin is usually discharged into a ditch. Current regulations allow for this ongoing discharge, but forthcoming regulations must designate certain pollutants and/or certain levels of these pollutants as hazardous pollution. is proposed.

For the removal of mercury and heavy metals from non-gaseous industrial wastewater streams, carbonates, phosphates or sulfur are often used to reduce hazardous pollutants to low residual levels. One known method of removing mercury and other hazardous pollutants from industrial wastewater streams is chemical precipitation reactions. Another known method uses ion exchange. One of the major problems with chemical precipitation reactions and ion exchange methods is that when the amount of contaminants is high (e.g. when processing fly ash slurry effluents), these methods become more demanding on non-gaseous effluents. This means that it cannot fully comply with EPA regulations for

Another source of polluted non-gaseous emissions is marine vessel wastewater and/or ballast water discharges. Commercial vessels such as cargo ships and tankers discharge both wastewater and ballast water. Recreational cruise ships also generate wastewater to be treated while in port. Additionally, military and defense vessels also produce significant amounts of wastewater.

Another large volume of wastewater is generated by offshore drilling operations. On-site wastewater treatment of offshore drilling rigs is significantly less expensive than transporting the wastewater ashore for treatment. Efficient filtration of marine wastewater prior to discharge into the sea is therefore necessary to maintain adequate and acceptable ecological requirements. Virtually all polluted effluents differ in the type and/or concentration of pollutants in the effluent. Therefore, a one-size-fits-all approach for suitable adsorbents optimized for all possible pollutant emissions is not possible. Application-specific sorbent solutions need to be considered to optimize effective effluent control based on the specific contaminants contained in the effluent. There is also a need to be able to adjust the sorbent application used in response to changes in the level and/or type of contaminants contained in the effluent during use.

There are also various known commercial emission control methods and systems sold under different trade names for treating secondary non-gaseous emissions. A treatment process known under the trade name Blue PRO is a reactive filtration process that uses co-precipitation and adsorption to remove mercury from secondary non-gaseous effluents. Another treatment method, known under the trade name MERSORB-LW, uses powdered coal-based sorbents to remove mercury from secondary non-gaseous effluents by co-precipitation and adsorption. Another treatment method, known as Chloralkali Electrolysis Wastewater, removes mercury from the secondary non-gaseous effluent during the electrolytic production of chlorine. Another treatment method uses absorption kinetics and activated carbon derived from fertilizer wastewater to remove mercury from secondary non-gaseous emissions. In another treatment method, polyethyleneimine-modified porous cellulose alone is used as an adsorbent to remove mercury from secondary non-gaseous effluents. Another treatment method uses microorganisms to remove mercury from the secondary non-gaseous effluent during enzymatic reduction. Yet another treatment method, known under the trade name MerCURxE, uses a chemical precipitation reaction to treat contaminated liquid non-gaseous effluents.

A treatment method found in some emissions control systems is to dilute the pollutants instead of removing them from the emissions. As a result, if the PPM level of a contaminant in the effluent exceeds an acceptable level, rather than removing this contaminant to reduce the level, additional non-pollutant is added to the effluent and accepted. While the actual amount of contaminants remains unchanged, it reduces the resulting PPM levels to acceptable levels. It is highly desired to overcome this dilution practice by providing an effective emission control method that not only lowers the PPM level of pollutants, but also removes pollutants from emissions.

This section provides a general summary of the disclosure and is not intended to be a comprehensive disclosure of its full scope or all features.

In one aspect of the present disclosure, an apparatus for removing contaminants from effluent is disclosed. The device comprises an inverted venturi-shaped housing. The housing has an inlet portion into which the discharged matter flows in at a predetermined inlet flow velocity, an outlet portion through which the discharged matter is discharged at a predetermined outlet flow speed, and a portion disposed between the inlet portion and the outlet portion of the housing. and an enlarged diameter portion for trapping contaminants in the air. The inlet section, outlet section and enlarged diameter section of the housing are arranged in fluid communication with each other. Additionally, the inlet portion of the housing has an inlet cross-sectional area, the outlet portion of the housing has an outlet cross-sectional area, and the enlarged diameter portion of the housing has an enlarged diameter cross-sectional area. Due to the inverted venturi shape of the housing, the enlarged diameter cross-sectional area is greater than the inlet cross-sectional area and the outlet cross-sectional area. Due to the shape of the housing, the effluent entering the enlarged diameter portion of the housing is decelerated and passes through the enlarged diameter portion of the housing at a lower speed relative to the speed at which it passes through the inlet and outlet portions of the housing. . Since the flow of effluent is slowed at the enlarged diameter portion of the housing, the residence time of the effluent in the enlarged diameter portion of the housing increases.

The device also has a reactant mass containing one or more adsorbents disposed within the enlarged diameter portion of the housing. The reactant mass has a reactive outer surface positioned to contact the effluent. Additionally, the reactant mass contains an amalgam-forming metal on the outer reaction surface. The amalgam-forming metal in the reactant mass chemically bonds with at least a portion of the contaminants in the effluent that reach the reactive outer surface of the reactant mass through the enlarged diameter portion of the housing. One or more sorbent recycling subsystems are disposed in communication with the housing. Each sorbent recycle subsystem takes in sorbent from the housing via a sorbent exhaust port and returns washed sorbent to the housing via a sorbent return port. The sorbent recycling subsystem contains chemical reagents that separate contaminants from the sorbent during the washing and regeneration steps before the washed sorbent is returned to the housing of the fluidized bed apparatus.

In another aspect of the present disclosure, an emission control method for removing pollutants from emissions is disclosed. The method comprises sending the effluent to a treatment system that includes an inverted venturi fluidized bed device containing one or more adsorbents that chemically bind contaminants contained in the effluent, and transferring the effluent to an inverted venturi fluidized bed device. sending in a direction away from. According to this method, the adsorbent is selected from a group of materials including copper, zinc, tin, sulfur (CZTS) adsorbents, copper, zinc, tin, sulfur (CZTS) alloy adsorbents, and carbon-based adsorbents. be. The method further includes routing the adsorbent through one or more chemical cleaning and adsorbent recycling subsystems for regeneration.

It is important to maintain optimum operating conditions for the adsorbents used to remove contaminated effluents from reverse venturi fluidized bed units. Therefore, the adsorbent is sent from the reverse venturi fluidized bed apparatus to the adsorbent recycling subsystem. The adsorbent recycle subsystem is designed to optimally wash and/or regenerate the adsorbent prior to returning the adsorbent to the inverted venturi fluidized bed apparatus. The adsorbent recycling subsystem is also designed to separate spent and exhausted adsorbents from other adsorbents that can be washed and/or regenerated and sent for disposal. The sorbent recycling subsystem is designed to further separate the captured contaminants from the sorbent for reuse in various industries or for proper disposal when no recycling options are available. Additionally, the sorbent recycling subsystem replenishes and/or replaces sorbent consumed during normal operations to remove separated sorbent and/or contaminants from the contaminated effluent for disposal. is designed to

According to another aspect of the present disclosure, the sorbent recycling subsystem includes one or more monitoring sensors that provide continuous in-line testing and monitoring feedback to maintain constant and consistent optimal sorbent conditions. In an exemplary embodiment of the present disclosure, three sorbent recycling subsystems are installed and configured in at least three separate locations. A first sorbent recycle subsystem is provided for the CZTS sorbent. A second adsorbent recycling subsystem is provided for the CZTS alloy adsorbent. A third sorbent recycling subsystem is provided for carbon-based sorbents. The specific effluent needs may determine which sorbent recycling subsystems are specifically needed. Depending on the level of contamination in the reverse venturi fluidized bed apparatus, the reverse venturi fluidized bed apparatus may be configured to use all three adsorbent recycling subsystems, or any of the adsorbent recycling subsystems may be used. or the same sorbent recycling subsystem may be located at multiple locations along the reverse venturi fluidized bed apparatus and used simultaneously.

In addition to the significant labor savings advantage, the apparatus and methods of the present application are more effective in removing hazardous pollutants from gaseous and non-gaseous emissions than known emission control systems and methods. These improvements are significant enough to enable industry to meet and/or exceed anticipated regulatory requirements, which are economically feasible with current technology. Impossible. Therefore, the apparatus and methods of the present application have the ability to continue to use fly ash even when regulations reclassify fly ash as a hazardous material, thereby enabling the construction industry, commercial power generation industry, and others. Significant cost increases can be prevented in industries that produce non-gaseous ash by-products.

Inverted Venturi fluidized bed devices have specific length/diameter ratios so that the effluent has an optimum confined residence time as it passes through a special adsorbent contained within the device. A specific size may be set as follows. By trial and error it has been found that the optimum length/diameter ratio of the housing of the fluidized bed apparatus is between 2.9:1 and 9.8:1, for example preferably 4.4:1. ing. Therefore, in an exemplary preferred embodiment. The diameter is 4.5 feet and the length is 19.8 feet, giving a length/diameter ratio of 4.4:1.

Another feature of the exemplary inverted venturi fluid bed apparatus is that it has a generally circular outwardly projecting convex end when viewed from both ends outside the enclosure. An example of a system having a fluidized bed apparatus configured in this manner was tested and found that the effluent flow was randomly reversed on its own side with minimal cavitational turbulence and no intimate contact. It has been demonstrated that the residence time (the time the effluent is in contact with the adsorbent) is maximized because it is maximized. The generally circular, outwardly projecting convex ends provide relatively smooth return flow at both ends of the fluidized bed apparatus, minimizing cavitational turbulence in the effluent. Turbulence associated with cavitation through filters is known to impede and/or disrupt flow. Extending the residence time in the fluidized bed apparatus is desirable for optimal capture of effluent contaminants and removal of contaminants from the effluent. However, extended residence time is not optimized if the flow is turbulent with cavitation. Various baffles and/or application-specific flow restricting obstructions may be provided in the housing of the fluidized bed apparatus.

In another aspect of the present disclosure, an exemplary contaminant removal system includes components made up of reconfigurable segments. Each system component may be isolated, bypassed, integrated, and/or reconfigured according to application-specific requirements.

According to another aspect of the present disclosure, an emissions control system comprises a fluidized bed of reactive adsorbent masses comprising copper, zinc, tin, sulfur (CZTS) adsorbents, CZTS alloys, and/or carbon-based adsorbents. Contained within the device. The fluidized bed apparatus also includes additional ports for washing and/or replacing the adsorbent material. Multiple sorbent recycling subsystems disclosed herein provide methods of using CZTS sorbents, CZTS alloy sorbents, and/or carbon-based sorbents. Exemplary emission control systems may also include pre-filters and/or post-filters that include one or more reactive sorbent masses. Depending on the specific needs of the application, multiple pre-filters and post-filters are connected in parallel or in series to the fluidized bed apparatus.

Emission pollutants from industrial applications include Hg (mercury), As (arsenic), Ba (barium), Cd (cadmium), Cr (chromium), Cu (copper), Pb (lead), Sn (tin) , P (phosphorus), NO2 (nitrogen dioxide), NO3 (nitrates), NH3 (ammonia). Such a long list of contaminants makes it impossible to have a one-size-fits-all emission control solution. Moreover, an emission control solution that works for one type of pollutant in gaseous emissions may not be effective for the same pollutants in non-gaseous emissions, and vice versa.

International regulatory standards, federal regulatory standards, state regulatory standards, and local regulatory standards establish various acceptable ppm levels of each pollutant in gaseous and/or non-gaseous emissions. Many of these regulatory standards set different allowable levels of pollutants depending on whether the pollutants are in gaseous or non-gaseous emissions.

Testing of contaminated effluents may involve spot checks and/or the use of continuous in-line monitoring equipment to determine the types and levels of contaminants contained in the effluents. Depending on the test results, the specific pre-filter and/or post-filter into which the contaminated effluent is introduced may be selected. Each pre-filter and/or post-filter contains a mass of specific reactive adsorbents targeted to specific contaminants contained in the effluent for a wide range of treatment options.

The types and/or levels of contaminants contained in the effluent change and/or fluctuate during the discharge of the effluent. Frequent and/or continuous in-line monitoring of contaminants allows specific pre-filters and/or Postfilter selection can be adjusted.

The present disclosure includes extensive tables that associate specific types of contaminants contained in gaseous and non-gaseous effluents with specific reactive adsorbents effective in capturing and removing the corresponding contaminants. . This table maps whether a particular reactive sorbent can be separated from a particular captured contaminant to recycle or dispose of the contaminant, and whether the sorbent can be regenerated and reused in an emission control system. show.

In addition to permanently installed systems for specific applications, the systems of the present application may be configured as transportable systems. Examples of transportable systems include, but are not limited to, truck-mounted systems, barge-mounted systems, trailer-mounted systems, and rail-mounted systems. Transportable systems are useful for bypassing field-built systems by providing temporary effluent bypasses, and for allowing permanent field-built systems to be serviced, serviced, and/or repaired. is. The transportable system is also useful to provide excess filtering capacity to permanent on-site equipment when the flow rate of contaminated effluent exceeds the capacity of the permanent on-site equipment.

There are numerous advantages of using the specialized adsorbents described herein with the disclosed apparatus and methods. In general, the ability of the effluent system disclosed by this sorbent to capture, contain and/or recycle mercury and other hazardous materials is previously not possible using known effluent control systems and methods. Another important advantage of the sorbents disclosed herein is that the sorbents can be used to treat both gaseous and non-gaseous effluents, thereby Many of the problems of known methods of treating polluted non-gaseous emissions, such as secondary emissions resulting from primary emission control treatments used, can be overcome. In addition, the sorbents described herein treat gaseous effluents sufficiently efficiently to obviate the need for secondary treatment of non-gaseous effluents produced as by-products of the primary gaseous effluent treatment process. gain the ability. The sorbents disclosed herein are also beneficial in that they are reusable. Hazardous contaminants that chemically bond with the amalgam-forming metals in the sorbent can be collected (i.e., removed) from the sorbent through regeneration treatment methods, thereby removing contamination from gaseous and/or non-gaseous effluents. Restores the sorbent's ability to remove material.

Further areas of applicability will become apparent from the description provided herein. The descriptions and specific examples in this summary are for illustrative purposes only and are not intended to limit the scope of the present disclosure.

The descriptions and specific examples in this summary are for illustrative purposes only and are not intended to limit the scope of the present disclosure.

Other advantages of the present invention will be readily appreciated by reference to the following detailed description in conjunction with the accompanying drawings. These drawings show:

1 is a schematic diagram showing a known configuration of a coal-fired power plant; FIG. 2 is a schematic diagram showing a known configuration of an emissions control system used to remove pollutants from emissions produced by a coal-fired power plant of the type shown in FIG. 1; FIG. 3 is a schematic diagram of the emissions control system shown in FIG. 2 and modified by adding an exemplary reverse venturi device constructed in accordance with the present disclosure; FIG. 1 is a side cross-sectional view of an exemplary reverse venturi device having a housing having an inlet section, an enlarged diameter section, and an outlet section, constructed in accordance with the present disclosure; FIG. 4B is a front cross-sectional view of the inlet portion of the housing of the exemplary reverse venturi device shown in FIG. 4A; FIG. 4B is a cross-sectional front view of the enlarged diameter portion of the housing of the exemplary inverted venturi device shown in FIG. 4A; FIG. FIG. 4B is a front cross-sectional view of the outlet portion of the housing of the exemplary reverse venturi device shown in FIG. 4A; FIG. 4 is a side cross-sectional view of another exemplary inverted venturi device having a series of alternating baffles disposed in the enlarged diameter portion of the housing to form a tortuous flow path for the exhaust, constructed in accordance with the present disclosure; FIG. 4 is a side cross-sectional view of another exemplary reverse venturi device constructed in accordance with the present disclosure and having a helical baffle disposed in the enlarged diameter portion of the housing to form a helical flow path for the exhaust. 6B is a front perspective view of the helical baffle of the exemplary inverted venturi device shown in FIG. 6A; FIG. FIG. 4 is a side cross-sectional view of another exemplary reverse venturi device having a plurality of spaced apart baffles disposed in the enlarged diameter portion of the housing, constructed in accordance with the present disclosure; FIG. 7B is a front cross-sectional view of the exemplary inverted venturi device shown in FIG. 7A taken along line AA, showing one orifice of the baffle; FIG. 4 is a side cross-sectional view of another exemplary inverted venturi device having a plurality of fragments disposed in the enlarged diameter portion of the housing, constructed in accordance with the present disclosure; FIG. 4 is a side cross-sectional view of another exemplary inverted Venturi device having a plurality of entangled threads disposed in an enlarged diameter portion of a housing to form a filament, constructed in accordance with the present disclosure; FIG. 4 is a side cross-sectional view of another exemplary inverted venturi device having a filter element disposed in the enlarged diameter portion of the housing, constructed in accordance with the present disclosure; FIG. 4 is a cross-sectional side view of another exemplary inverted venturi device constructed in accordance with the present disclosure, in which the enlarged diameter portion of the housing accommodates a plurality of baffles and a plurality of various sized debris disposed between adjacent baffles; FIG. 12 is a front view showing an example of a fragment sized to be accommodated in the enlarged diameter portion of the housing of the exemplary inverted venturi device shown in FIG. 11; FIG. 12 is a front view of another example of debris sized to be accommodated in the enlarged diameter portion of the housing of the exemplary inverted venturi device shown in FIG. 11; FIG. 12 is a front view of another example of debris sized to be accommodated in the enlarged diameter portion of the housing of the exemplary inverted venturi device shown in FIG. 11; FIG. 12 is a front view of another example of debris sized to be accommodated in the enlarged diameter portion of the housing of the exemplary inverted venturi device shown in FIG. 11; FIG. 12 is a front view of an example of an asterisk-shaped piece of loose material that can be used to replace the debris shown in the exemplary inverted venturi device shown in FIGS. 8 and 11 in combination with other pieces; FIG. 12 is a front view of an example of a crystalline flake that can be used to replace the fragments shown in the exemplary inverted venturi device shown in FIGS. 8 and 11 in combination with other crystalline flakes. FIG. 12 is a front view of one example of a wire coil that can be used to replace the debris shown in the exemplary inverted venturi device shown in FIGS. 8 and 11 in combination with other wire coils. FIG. 4 is a cross-sectional side view of another exemplary inverted venturi device having two separate flared portions connected in series and constructed in accordance with the present disclosure; FIG. 4 is a cross-sectional side view of another exemplary reverse venturi device having two separate parallel-connected flared portions constructed in accordance with the present disclosure; FIG. 4 is a side cross-sectional view of another exemplary reverse venturi device constructed in accordance with the present disclosure; 1 is a block flow diagram illustrating a known method of removing contaminants from gaseous emissions; FIG. 17 modified by adding the step of injecting the adsorbent into the gaseous effluent at a first introduction point and then passing the gaseous effluent through a reverse venturi device. FIG. 4 is a block diagram showing how to do this. 17 modified by adding the step of injecting the adsorbent into the gaseous effluent at a second introduction point and then passing the gaseous effluent through a reverse venturi device. FIG. 4 is a block diagram showing how to do this. 1 is a block diagram illustrating a known method of removing contaminants from non-gaseous effluent, which method requires settling the non-gaseous effluent in a sedimentation basin; FIG. 20 is a block diagram illustrating a known method for removing contaminants from non-gaseous effluent shown in FIG. 19 modified by adding a step of treating a portion of the non-gaseous effluent extracted from the sedimentation basin with an adsorbent; FIG. . 4 is a graph showing the percentage of contaminants removed from effluents by known emissions control systems and the percentage of contaminants removed from effluents by the apparatus and methods disclosed herein. FIG. 2 is a block flow diagram illustrating an exemplary method of removing contaminants from gaseous effluents and washing reactants to separate contaminants from gaseous effluents using an inverted venturi fluidized bed apparatus. FIG. 3 is a block flow diagram illustrating an exemplary method of removing contaminants from non-gaseous effluents and washing reactants to separate contaminants from non-gaseous effluents using an inverted venturi fluidized bed apparatus. FIG. 2 is a flow diagram illustrating extended non-turbulent effluent flow through an exemplary inverted venturi fluidized bed apparatus and exemplary method steps for washing and recycling adsorbents that separate contaminants from the effluent. In an exemplary method using an inverted venturi fluidized bed apparatus having a tilting mechanism mounted on a transportable pedestal deck, the enclosure of the inverted venturi fluidized bed apparatus is mounted on the pedestal to remove contaminants from the gaseous effluent. FIG. 4 is a block flow diagram showing parallel to the deck; In an exemplary method using an inverted venturi fluidized bed apparatus having a tilting mechanism mounted on a transportable pedestal deck, the enclosure of the inverted venturi fluidized bed apparatus includes: FIG. 4 is a block flow diagram showing a transverse orientation with respect to the cradle deck; 4 is a table that contrasts specific types of contaminants with the effectiveness of the disclosed CZTS alloy adsorbents as compared to activated carbon and zeolite adsorbents for gaseous and non-gaseous emissions. FIG. 4 is a schematic diagram showing an exemplary CZTS alloy sorbent compared to other exemplary types of sorbents for gaseous and non-gaseous emissions. Table showing prior art sorbents and their ability to separate and recycle contaminants in gaseous and non-gaseous effluents. 4 is a table showing the disclosed broad spectrum CZTS alloy sorbents and their ability to separate and recycle contaminants in gaseous and non-gaseous effluents. FIG. 2 is a block diagram showing how a contaminated gaseous effluent is routed through different filters containing specific effective adsorbents that match the type and/or level of contaminants contained in the gaseous effluent. FIG. 4 is a block diagram illustrating how a contaminated non-gaseous effluent is routed through different filters containing specific effective adsorbents that match the type and/or level of contaminants contained in the non-gaseous effluent. Extended non-turbulent effluent flow through an exemplary inverted Venturi fluidized bed apparatus and a series of adsorbent recycling subsystems for CZTS adsorbents, CZTS alloy adsorbents, and/or carbon-based adsorbents to remove contaminants FIG. 2 is a flow diagram showing exemplary method steps for washing and recycling the sorbent that separates from the effluent.

An apparatus and method for removing pollutants from industrial effluents will be described with reference to the drawings, wherein like numerals indicate corresponding elements throughout.

Exemplary embodiments are described more fully with reference to the accompanying drawings. This exemplary embodiment is provided so that this disclosure will be thorough, and will fully convey the scope to those skilled in the art. Numerous specific details are set forth, including examples of specific components, devices and methods, in order to provide a thorough understanding of the disclosed embodiments. It will be apparent to those skilled in the art that the specific details need not be used and that the example embodiments can be implemented in many different forms and should not be construed as limiting the present disclosure. In some exemplary embodiments, well-known methods, well-known device structures, and well-known techniques are not described in detail.

The terminology used herein is for the purpose of describing particular example embodiments only and is not intended to be limiting. As used herein, the singular is intended to include the plural unless explicitly stated otherwise. The terms "comprising", "comprising", "including" and "having" are inclusive and specify the presence of the stated features, integers, steps, acts, elements and/or parts. However, it does not exclude the presence or addition of one or more features, integers, steps, operations, elements, parts and/or groups. Method steps, processes and operations described herein should not be construed as requiring performance in the particular order described or illustrated, unless specifically specified as an order of performance. Of course, additional or alternative steps may be used.

When an element or layer is referred to as being "on", "engaging with", "connected to" or "coupled to" another element or layer, that element or layer is directly on the other element or layer. may be in, engage, connect or couple. Alternatively, there may be intervening elements or layers. On the other hand, when an element is referred to as being "directly on," "directly engaging with," "directly connected to," or "directly connected to," another element or layer, there are no intervening elements or layers. you can Other terms used to describe relationships between elements (e.g., "between" and "directly between," "adjacent" and "directly adjacent," etc.) should be construed in the same manner. It should be. As used herein, the term "and/or" includes all combinations of one or more associated list items.

Although the terms first, second, third, etc. are used herein to describe various elements, components, regions, layers and/or sections, these elements, components, regions, layers and/or Cutting planes are not limited by these terms. These terms may only be used to distinguish one element, component, region, layer and/or section from another region, layer or section. Terms such as "first," "second," and other numerical terms when used herein do not imply an arrangement or order, unless the context clearly indicates. Thus, first elements, components, regions, layers and/or cut surfaces discussed below may be referred to as second elements, components, regions, layers and/or cut surfaces without departing from the teachings of the examples. is also possible.

Spatially relative terms such as "inner", "outer", "beneath", "beneath", "below", "above", "above", etc. are used in the illustrations. May be used herein to facilitate describing the relationship of an element or feature to other elements or features. Spatially relative terms may encompass different orientations of the device in use or operation in addition to the orientation shown. For example, when the device in the figures is turned over, an element described as "below" or "beneath" another element or feature would be placed "above" the other element or feature. Thus, the exemplary term "below" can encompass both up and down orientations. The device may be oriented in other directions (rotated 90 degrees or in other orientations) and the spatially related descriptions used herein should be construed accordingly.

The term "conduit" as used herein is intended to cover the description of all pipes normally available for carrying liquids and/or liquid effluents and gases and/or gaseous effluents. is. No preference is given or implied as to the actual method of transporting any Emission regardless of the type of Emission. Additionally, the terms "contaminate(s)" and "contaminant(s)" are used interchangeably in this disclosure.

Referring to FIG. 1, a schematic diagram of a typical coal-fired power plant 100 is shown. This coal-fired power plant 100 has a fluidized bed reactor 1 which is an industrial installation that burns one or more coal fuels 2 to generate electricity 7 . This power 7 may then be distributed to the grid via wires 8 . Combustion in the fluidized bed reactor 1 is carried out by air 3 , fire 4 and coal fuel 2 . This combustion process is used to heat water and generate steam 5 . This steam is then used to turn a generator 6 to generate electricity 7 . Gaseous emissions 10 from the combustion process are discharged into the environment through a chimney 9 . If no emissions control system were installed in the coal-fired power plant 100 (FIG. 1), the emissions 10 would be fly ash, mercury (Hg), metal vapors, sulfur dioxide (SO2), hydrogen chloride (HCl) and Contains many harmful pollutants such as other noxious gases.

Referring to FIG. 2, a schematic diagram of a modified coal-fired power plant 200 having a conventional emissions control system 202 is shown. The emissions control system 202 traps and collects a portion of the hazardous pollutants in the gaseous emissions 10 . This effluent control system 202 includes a wet/dry scrubber 11 that removes some of the sulfur dioxide and fly ash contaminants from the gaseous effluent 10 from the fluidized bed reactor 1 in which the combustion reaction takes place. transport to Alternatively, or in addition to conveying the gaseous effluent 10 to the wet/dry scrubber 11, the emissions control system 202 may remove the gaseous effluent 10 from sulfur dioxide, noxious gases and one of other pollutants. It may be conveyed to a jet dryer 12 where the parts are caught and collected. This effluent may be passed through a textile filter unit 13 (or baghouse) that removes particles from the stream of gaseous effluent 10 using filter bags. This system collects and removes many pollutants from the gaseous effluent 10 before it is discharged through the chimney 9 into the surrounding atmosphere (ie, the environment). A problem with the conventional emission control system 202 shown in FIG. machine 12 and fiber filter unit 13.

Referring to FIG. 3, there is shown a schematic diagram of a modified coal-fired power plant 300 having an sorbent injector 14 and a reverse venturi device 15 in addition to the emissions control system 202 shown in FIG. The sorbent injector 14 operates to add sorbent to the gaseous effluent 10 and may be positioned upstream of the reverse venturi device 15 . More specifically, in the example shown in FIG. 3, the sorbent injector is positioned between the jet dryer 12 and the fiber filter unit 13 . In FIG. 3 the reverse venturi device 15 is positioned between the fiber filter unit 13 and the chimney 9, although different positions of the reverse venturi device 15 are possible. One of the major advantages of this arrangement is that the reverse venturi device 15 can be installed in existing installations, requiring only a "Modification to Existing Permit" to be applied, and a completely new emission control system. It saves both time and money compared to applying for a system. In operation, gaseous effluent 10 is directed from fiber filter unit 13 to reverse venturi device 15 . As will be described in more detail below, this reverse venturi device 15 is provided with internal structures suitable for collecting and trapping substantial quantities of mercury, heavy metals, nano-sized particles and other contaminants. The gaseous effluent 10 exiting the chimney 9 is therefore substantially free of all harmful pollutants.

As shown in Figures 4A-4D, the inverted venturi device 15 has a housing 16 that is in the shape of an inverted venturi. Note that a venturi is generally described as a conduit that first contracts from a larger cross-section to a smaller cross-section and then expands from the smaller cross-section to a larger cross-section. Accordingly, the term "inverted venturi" as used herein means the opposite, i.e., a conduit that first expands from a smaller cross-section to a larger cross-section and then contracts from the larger cross-section to a smaller cross-section. . Specifically, the housing 16 of the disclosed inverted venturi device 15 extends along a central axis 17 and has an inlet section 18 , an enlarged diameter section 19 and an outlet section 20 . The inlet portion 18 of this enclosure 16 is sized such that the gaseous effluent 10 enters at a predetermined inlet flow velocity characterized by an inflow velocity V1 and a pressure P1. The outlet section 20 of this enclosure 16 is sized such that the gaseous effluent 10 exits at a predetermined outlet flow rate characterized by an outlet velocity V3 and a pressure P3. This enlarged diameter portion 19 is located between the inlet portion 18 and the outlet portion 20 of the housing 16 and forms an enlarged diameter chamber 21 therein for trapping contaminants in the gaseous exhaust 10 . The enlarged diameter portion 19 of the housing 16 has an inner surface 68 approximately facing the central axis 17 . The inlet portion 18, the enlarged diameter portion 19, and the outlet portion 20 of the housing 16 are in fluid communication with each other along the central axis 17. are arranged in order to That is, inlet portion 18 , enlarged diameter portion 19 , and outlet portion 20 of housing 16 together form a conduit extending along central axis 17 .

Inlet 18 of housing 16 has an inlet cross-sectional area A 1 transverse to central axis 17 and outlet 20 of housing 16 has an outlet cross-sectional area A 3 transverse to central axis 17 . The inlet cross-sectional area A1 may be equal (ie, identical) to the outlet cross-sectional area A3 such that the predetermined inlet flow rate is equal (ie, identical) to the predetermined outlet flow rate. Alternatively, the inlet cross-sectional area A1 and the outlet cross-sectional area A3 are different (i.e., smaller or larger) such that the predetermined inlet flow rate is different (i.e., smaller or larger) than the predetermined outlet flow rate. ) is also good. As used herein, the term "flow rate" refers to the volumetric flow rate of the effluent.

Enlarged diameter portion 19 of housing 16 traverses central axis 17 and has an enlarged diameter cross-sectional area A2 that is greater than inlet cross-sectional area A1 and outlet cross-sectional area A3. Therefore, the enlarged diameter portion 19 is such that the flow velocity V2 of the exhaust gas 10 in the enlarged diameter portion 19 of the housing 16 is smaller than the flow velocity V1 of the exhaust gas 10 in the inlet portion 18 of the housing 16, and It is sized to be less than the flow velocity V3 of the gaseous effluent 10 in the outlet 20 of the body 16 . Such a decrease in flow velocity increases the residence time of the exhaust gas 10 within the enlarged diameter portion 19 of the housing 16 . As used herein, the term "residence time" refers to the average amount of time required for molecules within gaseous exhaust 10 to pass through enlarged diameter portion 19 of housing 16. FIG. That is, the "residence time" of the enlarged diameter portion 19 of the housing 16 is equal to the time required for all the discharges in the enlarged diameter chamber 21 to be renewed. Also, as used herein, the term "cross-sectional area" refers to an internal cross-sectional area (ie, the space inside housing 16) that is the same regardless of changes in housing 16 thickness. Accordingly, the expanded diameter section cross-sectional area A2 reflects the size of the expanded diameter chamber 21 and is defined by the inner surface 68 .

Due to the shape of the housing 16, the internal pressure P1 of the gaseous emissions 10 passing through the inlet 18 of the housing 16 and the internal pressure P3 of the gaseous emissions 10 passing through the outlet 20 of the housing 16 are It is greater than the internal pressure P2 of the gas discharge 10 passing through the enlarged diameter portion 19 . The flow velocity V2 of the gas emission 10 in the enlarged diameter portion 19 of the housing 16 is smaller than the flow velocity V1 of the gas emission 10 at the inlet 18 of the housing 16, and the gas discharge at the outlet 20 of the housing 16. This pressure differential, combined with the fact that the flow velocity of the material 10 is less than V3, causes the gaseous exhaust material 10 to accumulate in the enlarged diameter portion 19 of the housing 16 . As a result of the pressure and velocity differentials described above, and because the gas discharge 10 will naturally expand to occupy the entire volume of the expanded diameter chamber 21, the gas discharge 10 within the enlarged diameter portion 19 of the housing 16 will will be subjected to an expansion force. This fact, combined with effects due to laminar flow, pneumatic dynamics, and gas behavior physics, effectively removes Increased ability to capture and thereby remove contaminants.

Housing 16 may have a variety of different shapes and configurations. As a non-limiting example, inlet section 18, enlarged diameter section 19, and outlet section 20 of housing 16 shown in FIGS. 4A-4D all have circular cross-sectional areas A1, A2, A3. Alternatively, the cross-sectional areas A1, A2, A3 of one or more of the inlet portion 18, the enlarged diameter portion 19 and the outlet portion 20 of the housing 16 may be non-circular, and may be of circular and non-circular cross-sections. Various combinations are possible and are considered within the scope of this disclosure. In some constructions, the enlarged diameter portion 19 of the housing 16 may have a diverging end 22 and a converging end 23 . According to these structures, the enlarged diameter portion 19 of the housing 16 tapers outward from the inlet cross-sectional area A1 to the enlarged diameter cross-sectional area A2 at the divergent end 22 . That is, the cross-section of the enlarged diameter portion 19 of the housing 16 increases at the divergent end 22 as it moves away from the inlet portion 18 of the housing 16 . On the other hand, the enlarged diameter portion 19 of the housing 16 tapers gradually inward at the converging end 23 from the enlarged diameter portion cross-sectional area A2 to the outlet cross-sectional area A3. That is, the cross section of the enlarged diameter portion 19 of the housing 16 becomes smaller at the converging end 23 as it moves in the direction toward the exit portion 20 of the housing 16 . Accordingly, the gaseous emissions 10 within the enlarged diameter portion 19 of the housing 16 flow approximately from the diverging end 22 to the converging end 23 . In embodiments in which the inlet portion 18, the enlarged diameter portion 19, and the outlet portion 20 of the housing 16 all have circular cross-sectional areas A1, A2, A3, the diverging and converging ends 22, 23 of the housing 16 are approximately It may be conical. Notwithstanding the above, the diverging and converging ends 22, 23 of the enlarged diameter portion 19 of the housing 16 may be differently shaped. As a non-limiting example, the diverging and converging ends 22, 23 are designed to be more manufacturable without significantly adversely affecting the flow of the gaseous exhaust 10 through the housing 16 of the reverse venturi device 15. , may be polygonal. In another alternative configuration, the enlarged diameter portion 19 of the housing 16 resembles a sausage with relatively abrupt transitions between the inlet portion 18 and the diverging end portion 22 and between the converging end portion 23 and the outlet portion 20 . You may have a shape. It is presumed that smooth transitions are preferable to abrupt transitions because the laminar flow behavior of the gaseous exhaust 10 is more favorable. However, minor disturbances to the laminar flow of the gaseous discharge 10 during abrupt changes are not considered to be an absolute problem, but rather can result in better flow in areas where increased residence time is not required. There is also sex.

With continued reference to FIGS. 4A-4D and further to FIGS. 5-11, reactant mass 24 is positioned within enlarged diameter portion 19 of housing 16 . This reactant mass 24 has a reactive outer surface 25 that is positioned to contact the gaseous effluent 10 . Additionally, this reactant mass 24 chemically bonds with at least a portion of the contaminants in the gaseous effluent 10 that pass through the enlarged diameter portion 19 of the housing 16 to reach the reacting outer surface 25 of the reactant mass 24 . It contains an amalgam-forming metal on its reactive outer surface 25 . In this way, contaminants bound to the outer reaction surface 25 of the reactant mass 24 remain trapped within the enlarged diameter portion 19 of the housing 16 and thus flow out of the enlarged diameter portion 19 of the housing 16. are removed from the stream of gaseous effluent 10 entering the outlet 20 of the housing 16 . As used herein, the term “amalgam-forming metal” means a material selected from the group of metals capable of forming compounds with one or more of the contaminants in the gaseous effluent 10 . By way of non-limiting example, the amalgam-forming metal may be zinc and the contaminant in the gaseous effluent 10 may be mercury, whereby the gaseous effluent 10 contacts the reaction outer surface 25 of the reactant mass 24. In some cases, an amalgam of zinc and mercury may be formed.

The enlarged diameter portion 19 of the housing 16 allows a predetermined inlet flow rate while ensuring a sufficiently long residence time for the amalgam-forming metals in the reactant mass 24 to chemically bond with the contaminants in the gaseous effluent 10. of gaseous effluent 10. Therefore, to achieve this balance, the expanded cross-sectional area A2 may range from 3 square feet to 330 square feet to achieve dwell times ranging from 1 second to 2.5 seconds. This particular residence time is necessary to allow sufficient time for the contaminants in the gaseous effluent 10 to chemically bond with the amalgam-forming metals in the reactant mass 24 . Thus, a range of enlarged section cross-sectional areas A2 has been calculated to achieve this residence time in coal-fired power plants 100 with outputs ranging from 1 megawatt (MW) to 6000 megawatts (MW). As known in the chemical arts, the amalgam-forming metal can be a variety of different metals. As a non-limiting example, the amalgam-forming metal may be selected from the group consisting of zinc, iron and aluminum. Housing 16 is made of a different material than reactant mass 24 . As non-limiting examples, housing 16 may be made of steel, plastic or fiberglass.

Reactant mass 24 may have a variety of different, non-limiting configurations. In FIG. 4A, reactant mass 24 is shown as coating inner surface 68 of housing 16 . Alternatively, as shown in FIGS. 5-11, reactant mass 24 may form one or more obstruction elements 26a-26j disposed within enlarged diameter portion 19 of housing 16. FIG. These obstruction elements 26 a - 26 j as such form a tortuous flow path 27 for the gas exhaust 10 passing through the enlarged diameter portion 19 of the housing 16 . Obstruction elements 26 a - 26 j thus increase the residence time of gaseous exhaust 10 passing through enlarged diameter portion 19 of housing 16 . In some of the embodiments described below, the flow of gas exhaust 10 passing through the enlarged diameter portion 19 of the housing 16 is completely disrupted, so that the meandering flow paths 27 formed are completely random, This greatly increases the chances of chemical reactions between the contaminants in the gaseous effluent 10 and the amalgam-forming metals in the reactant mass 24 .

Each obstruction element 26a-26j of the structures shown in FIGS. 5-11 has a large surface area, which increases the reactive outer surface 25 of the reactant mass 24. FIG. It collects and traps contaminants in the enlarged diameter portion 19 of the housing 16 by chemical reaction between the amalgam-forming metals in the reactive outer surface 25 of the reactant mass 24 and the contaminants in the gaseous effluent 10 . Advantageously, and/or collectible, contaminants are removed from the gaseous effluent 10 . Therefore, the amount of contaminants that can be removed from the gaseous effluent 10 passing through the diametrically enlarged chamber 21 by the diametrically enlarged portion 19 of the housing 16 is determined by proportional to the size of 25. In addition, the complex surface geometry and/or texture of the obstruction elements 26a-26j may prevent contaminant entrapment, whether or not contaminant entrapment is the result of a chemical reaction between the contaminant and the amalgam-forming metal. Additional surface area is provided to facilitate physical trapping.

Referring again to FIG. 3, the sorbent added to the effluent by sorbent injector 14 includes amalgam-forming metals. The amalgam-forming metals in the adsorbent chemically bond with at least some contaminants in the gaseous effluent 10 before the gaseous effluent 10 enters the enlarged diameter portion 19 of the housing 16 . The sorbent may be, for example, zinc (Zn) powder or a copper-zinc-tin-sulfur (CZTS) compound, although the sorbent may have many different compositions. Because the sorbent chemically bonds with at least some of the contaminants in the gaseous effluent 10 before the gaseous effluent 10 enters the enlarged diameter portion 19 of the housing 16, the sorbent causes the reactant mass to Removal of contaminants from the gaseous effluent 10 by 24 is facilitated.

As shown in FIG. 5, obstruction elements 26 a - 26 j are provided as a series of interleaved baffles 26 a extending from inner surface 68 of enlarged diameter portion 19 of housing 16 . This series of interleaved baffles 26a traverses the central axis 17 and gives the meandering channel 27 a serpentine shape. The serpentine shape of this meandering channel 27 increases the residence time of the gaseous effluent 10 within the enlarged diameter portion 19 of the housing 16, thereby causing the gaseous effluent by the reactant masses 24 to form a series of interleaved baffles 26a. The capture and removal of contaminants in 10 is facilitated. In one example, this series of alternating baffles 26a is made of zinc. In another example, the series of alternating baffles 26a are of a material other than zinc coated with zinc. The arrangement of interleaved baffles 26a need not be evenly spaced or symmetrical along the length of central axis 17; This is because in some applications a wider space between adjacent baffles 26a is preferred and in other applications a narrower space between adjacent baffles 26a is preferred. Also, this series of interleaved baffles 26a may be replaced and/or cleaned as needed if they become saturated during operation of the reverse venturi device 15 .

As shown in FIGS. 6A and 6B, at least one obstruction element 26a-26j may be a helical baffle 26b. The helical baffle 26b extends along the central axis 17 and spirally within the enlarged diameter portion 19 of the housing 16 with the central axis 17 as the center. Therefore, the spiral baffle 26b causes the curved flow path 27 to have a spiral shape. The helical shape of this tortuous channel 27 increases the residence time of the gaseous effluent 10 within the enlarged diameter portion 19 of the housing 16, thereby reducing the amount of gaseous effluent 10 in the gaseous effluent 10 by the reactant mass 24 forming the helical baffle 26b. contaminant capture and removal is facilitated. In one example, this spiral baffle 26b is made of zinc. In another example, the helical baffle 26b is made of a material other than zinc coated with zinc. In yet another example, the helical baffle 26b is mechanically driven to rotate within the enlarged diameter portion 19 of the housing 16 about the central axis 17. As shown in FIG. By rotating the spiral baffle 26b, the flow of gaseous exhaust through the enlarged diameter portion 19 of the housing 16 can be artificially accelerated or decelerated depending on the direction of rotation of the spiral baffle. This helical baffle 26b may be replaced and/or cleaned as necessary if it becomes saturated during operation of the reverse venturi device 15 .

As shown in FIGS. 7A and 7B, at least one obstruction element 26a-26j is a plurality of baffles 26c. Each baffle 26 c extends from the inner surface 68 of the enlarged diameter portion 19 of the housing 16 across the enlarged diameter portion 19 of the housing 16 . The baffles 26c are spaced apart along the central axis 17 and each baffle 26c has an orifice 28 that permits the flow of gaseous exhaust 10 past the baffle 26c. Of course, any number of baffles 26c may be provided, including configurations having only a single baffle 26c. The size, shape and number of orifices 28 in each baffle 26c can vary. For example, baffle 26c may be screen-like and orifice 28 may be provided between the crosshairs of the screen. The orifice 28 in this baffle 26c restricts the flow of the gaseous effluent 10 within the enlarged diameter portion 19 of the housing 16 and increases the residence time of the gaseous effluent 10 within the enlarged diameter portion 19 of the housing 16. FIG. This facilitates the capture and removal of contaminants from gaseous exhaust 10 by reactant mass 24 forming baffle 26c. In one example, this baffle 26c is made of zinc. In another example, this baffle 26c consists of a material other than zinc coated with zinc. This baffle 26c may be replaced and/or cleaned as necessary if it becomes saturated during operation of the reverse venturi device 15. FIG. In yet another example, the size of orifice 28 in one baffle 26c differs from the size of orifice 28 in an adjacent baffle 26c. The use of different sized orifices 28 in different baffles 26c accelerates and/or restricts the flow of gaseous effluent 10 and allows the trapping and removal of contaminants in gaseous effluent 10 by reactant masses within baffles 26c. Promoted. Similarly, the baffles 26c need not be evenly spaced within the expanded chamber 21 and the orifice 28 of one baffle 26c is the same size, shape or location as the orifice 28 of an adjacent baffle 26c. No need. By varying the size, shape and location of these orifices 28 from one baffle 26c to another baffle 26c, and by varying the spacing of the baffles 26c, residence time of gaseous effluent 10 can be increased to facilitate increased contact with physical and chemical trapping and collection points along reactant mass 24 .

In another configuration shown in FIGS. 8-11, at least one obstruction element 26a-26j may not be fixed to housing 16 itself, but instead be free to extend within enlarged diameter portion 19 of housing 16. may be placed. In such configurations, at least one obstruction element 26a-26j may include various forms of obstruction media 26d-26j. Like the obstruction elements 26a-26c, the obstruction media 26d-26j may be of zinc or of a material other than zinc coated with zinc. Zinc is readily soluble and can be cast into complex shapes using conventional molding methods, loss wax methods, centrifugation methods, and the like. Other forming methods include cutting, extrusion, sintering, stamping, hot forging and forming, laser cutting, and the like. Alternatively, steel may be used for prototyping and then coated or plated with zinc as a surface cover. This obstruction medium 26d-26j can be used to completely fill the entire expanded chamber 21, partially fill the expanded chamber 21, or fill between the baffles 26c previously described in connection with FIGS. 7A and 7B. It is possible.

FIG. 8 shows a configuration in which at least one obstruction element 26 a - 26 j is a plurality of debris 26 d contained within enlarged diameter portion 19 of housing 16 . According to this configuration, the gaseous emissions 10 are separated from the adjacent fragments 26d as the gaseous emissions 10 move through the enlarged diameter portion 19 of the housing 16 from the inlet portion 18 of the housing 16 toward the outlet portion 20. pass through the space between For this reason, the plurality of fragments 26 d may be irregular in shape so that the fragments 26 d are loosely packed within the enlarged diameter portion 19 of the housing 16 . As a non-limiting example, the plurality of pieces 26d may consist of mossy zinc. Modi zinc is a popcorn-shaped zinc structure that is produced by immersing molten zinc in a cooling liquid such as water. The resulting droplets of molten zinc solidify into relatively small, spherical structures with a very high surface area to volume ratio. Additionally, the surface area of the resulting structure has a mossy surface texture. These structures can be sized for specific applications. By working steel, it is possible to produce composite spherical structures of steel plates similar to modzii zinc, which may be coated with zinc.

The loose packing of these multiple fragments 26d in FIG. 8 results in a random shape of the tortuous channel 27, which increases the residence time of the gaseous exhaust 10 within the enlarged diameter portion 19 of the housing 16. do-. This facilitates the capture and removal of contaminants from the gaseous effluent 10 by the reactant mass 24 forming a plurality of fragments 26d. This plurality of debris 26d in FIG. 8 may be replaced and/or cleaned as needed if it becomes saturated during operation of the reverse venturi device 15. FIG.

In another configuration shown in FIG. 9, at least one of the obstructing elements 26a-26j is a plurality of entangled threads 26e housed within the enlarged diameter portion 19 of the housing 16. As shown in FIG. The plurality of entangled threads 26 e form a thread-like body within the enlarged diameter portion 19 of the housing 16 . In one possible configuration, the plurality of entangled threads 26e are folded and rolled like steel wool to form a clump with a very large surface area. The entangled yarns 26e themselves may be of the same composition, thickness and length, or may be a combination of different compositions, thicknesses and/or lengths. In one example, these multiple entangled yarns 26e consist of zinc wires and are randomly entangled to form zinc wool. This zinc wool can be made from wires of varying levels of density and/or size to impart specific flow restriction capabilities. In another example, these multiple entangled yarns 26e consist of steel wires that are randomly entangled to form steel wool. This steel wool may be coated with zinc. The loose packing of these multiple entangled threads 26e in FIG. increases. This facilitates the capture and removal of contaminants in gaseous exhaust 10 by reactant mass 24 forming entangled threads 26e. These multiple entangled threads 26e may be replaced and/or cleaned as needed if they become saturated during operation of the reverse venturi device 15 .

Referring to FIG. 10, another configuration is shown in which at least one obstructing element 26a-26j is a filter element 26f. The filter element 26 f extends across the enlarged diameter portion 19 of the housing 16 with respect to the central axis 17 . The filter element 26f is porous and the pores in the filter element 26f allow the gaseous exhaust 10 to flow through the enlarged diameter portion 19 of the housing 16 from the inlet 18 to the outlet 20 of the housing 16. It is allowed to pass through the filter element 26f. This configuration of the filter element 26f, which may be of sintered metal, results in a random shape of the tortuous flow path 27, which increases the residence time of the gaseous effluent 10 passing through the enlarged diameter portion 19 of the housing 16. FIG. This facilitates the capture and removal of contaminants in gaseous exhaust 10 by reactant mass 24 forming filter element 26f. The sintered metal of filter element 26f preferably comprises zinc or a non-zinc material coated with zinc. This filter element 26f may be replaced and/or cleaned as necessary if it becomes saturated during operation of the reverse venturi device 15. FIG.

Referring to FIG. 11, as a combination of baffles 26c shown in FIGS. 7A and 7B and fragments 26g-26j of different sizes and similar to fragments 26d shown in FIG. At least one obstruction element 26a-26j is shown. According to this alternative configuration, the plurality of baffles 26c and the plurality of fragments 26g-26j are located within the enlarged diameter portion 19 of the housing 16. FIG. Similar to FIGS. 7A and 7B, the plurality of baffles 26c shown in FIG. Further, the plurality of baffles 26c are spaced apart from each other along the central axis 17 such that the baffles 26c divide the expanded diameter chamber 21 into a plurality of compartments. An orifice 28 in each baffle 26c allows the flow of gaseous effluent 10 to pass through the baffle 26c. A plurality of fragments 26g-26j are positioned between adjacent baffles 26c (ie, positioned within the plurality of compartments of expanded diameter chamber 21).

A plurality of fragments 26g-26j form reactant mass 24, as shown in FIGS. 11 and 12A-12D. These plurality of pieces 26g-26j are of different sizes, grouped with pieces of the same size (i.e., pieces 26g, 26h, 26i, and 26j are grouped separately), and pieces of different sizes. may be separated by baffle 26c. For example, groups of fragments 26g-26j may be arranged such that the size of fragments 26g-26j move away from inlet 18 of housing 16 and decrease in size as they approach outlet 20 of housing 16. FIG. That is, the size of each group of fragments 26g-26j may be gradually varied so that the gaseous emissions 10 are reduced in the overall direction of flow within the enlarged diameter portion 19 of the housing 16. FIG. In one example, the pieces 26g-26j are made of zinc. For example, fragments 26g-26j can be formed by dropping molten zinc into a coolant to create popcorn-shaped structures with very large surface areas and random mossy textures. In another example, pieces 26g-26j of different sizes may be mixed together and not separated based on size.

In Figures 13A-13C, several alternative forms of obstruction elements 26k-26m are shown as incompressible material, which may be in addition to or in addition to fragments 26d and 26g-26j shown in Figures 8 and 11 . can be used instead of FIG. 13A shows an example where an obstacle 26k forms a reactant mass 24 and has an asterisk shape resembling "Jacks" children's toys. FIG. 13B shows another form of obstruction elements 26k-26m forming reactant mass 24 and positioned in enlarged diameter portion 19 similar to housings 16 and 26g-26j shown in FIGS. An example is shown which is a plurality of crystalline flakes 261 (only one is shown). This crystal flake 261 has a shape similar to a snowflake. FIG. 13C shows another form of obstruction elements 26k-26m are a plurality of wire coils 26m (only one shown) forming reactant mass 24 and housings 16 and 26g shown in FIGS. -26j, it may be placed in the enlarged portion 19 as an example. Obstacle 26k and plurality of crystal flakes 261 are made of zinc or a non-zinc material coated with zinc such as, but not limited to, lost wax forging and 3D printing. Also good. The plurality of wire coils 26m are formed by, for example, zinc wire being spring-wound around a mandrel core and then cutting the entire coil of wound wire along the entire length of the mandrel core to form rings of individual coils. may be made by obtaining The differently shaped obstruction elements 26k-26m may or may not completely fill the expanded chamber 21. As shown in FIG.

Various combinations of the various obstruction elements 26a-26k described above may be intermixed. An example of this mixed combination is one or more baffles 26a-26c shown in FIGS. including combining with Another example of a mixed combination includes combining multiple entangled yarns 26e shown in FIG. 9 with multiple pieces 26d and 26g-26j shown in FIGS. Other configurations are possible that combine the various obstruction elements 26a-26k described above with other filter elements such as activated carbon. Activated carbon, like a sponge, collects contaminants by surface contact. Accordingly, a limited amount of activated carbon may be introduced into the enlarged diameter portion 19 of the housing 16 to work with the various obstruction elements 26a-26k described above. Preferably, the obstruction elements 26 a - 26 k retain the activated carbon within the enlarged diameter portion 19 of the housing 16 such that the activated carbon is relatively statically distributed throughout the enlarged diameter chamber 21 . This configuration is contrary to conventional emission control systems that release activated carbon into the stream of gaseous emissions 10 . Activated carbon can be used more efficiently because it does not flow freely with the gaseous effluent. Those skilled in the art will appreciate that the disclosed examples of reverse venturi devices 15 are merely exemplary, and that numerous combinations beyond the few examples disclosed herein are possible and desirable to accommodate particular applications. you will easily understand.

Referring to FIG. 14, another exemplary reverse venturi device 15' comprising two enlarged diameter portions 19, 19' connected in series by a conduit 38 is shown. One enlarged diameter portion 19 of housing 16 extends between inlet portion 18 of housing 16 and conduit 38 and the other enlarged diameter portion 19 ′ extends between conduit 38 and outlet portion 20 of housing 16 . Extend. The tortuous path 27 of the gas discharge 10 is thus elongated. With this arrangement, the gaseous effluent 10 is channeled from the enlarged diameter portion 19 through the conduit 38 to the enlarged diameter portion 19' where further contaminants are collected and/or captured. The present disclosure is not limited to using only one or two flares 19, 19' in series. This is because in some applications with large emissions and/or high levels of pollutants, it may be necessary to connect a large number of flares in series.

Referring to FIG. 15, there is shown another exemplary inverted venturi device 15'' comprising two enlarged diameter portions 19, 19'' connected in parallel. A three-way inlet valve 39 controls the flow of gaseous effluent 10 and allows gaseous effluent 10 to enter conduit 41 or conduit 42 . Three-way outlet valve 40 allows gaseous exhaust 10 to flow out of conduit 41 or conduit 42 without direct backflow from conduit 41 to conduit 42 or from conduit 42 to conduit 41 . Gas effluent 10 flows from inlet 18 into enlarged diameter 19 and out of outlet 20 as gas effluent 10 is directed through conduit 41 . Gas effluent 10 flows from inlet 18 ″ into enlarged diameter 19 ″ and out of outlet 20 ″ as gas effluent 10 is directed from conduit 42 . One of the advantages of this reverse venturi device 15'' shown in FIG. 15 is that maintenance of one of the flares 19, 19'' is not required because the other one of the flares 19, 19'' can remain operational. , if repair or cleaning is required, it can be isolated and taken offline without shutting down the entire system.

Over time, chemical reactions and/or physical entrapment of contaminants on the outer reaction surface 25 of the reactant mass 24 can cause the reactant mass 24 to reach a saturation point and reduce the efficiency of the reverse venturi device 15 . have a nature. Thus, in the configuration shown in FIG. 15, the removal, replacement and/or cleaning of the reactant mass 24 within the enlarged diameter portion 19, 19'' of the housing 16 allows the reverse venturi device to be operated without a complete shutdown. can be restored to the efficiency before saturation.

The process of removing contaminants from the saturated reactant mass depends on the specific contaminant type and the type of amalgam-forming metal used. Access to the enlarged diameter chambers 21, 21'' located inside the enlarged diameter portions 19, 19'' of the housing 16 depends on the type of obstacle used. If relatively small, incompressible obstructions are used, a pouring and/or draining type of access is required. If the obstacle is a relatively large block, plate, baffle or assembly, proper lifting and handling methods and access are required.

Still referring to FIG. 15 , the reverse venturi device 15 may have one or more spray nozzles 81 in fluid communication with the enlarged diameter portions 19 , 19 ″ of the housing 16 . The spray nozzle 81 is positioned to spray deoxygenated acid onto the reactant mass 24 within the enlarged diameter portion 19 , 19 ″ of the housing 16 . In operation, the oxygen scavenger flushes contaminants from the reactant mass 24 to rejuvenate the reactant mass 24 . Alternatively, drain 82 may be in fluid communication with enlarged diameter portions 19, 19'' of housing 16 to carry spent oxygen scavengers and contaminants out of enlarged diameter portions 19, 19'' of housing 16. can be Saturated zinc, whether coated on steel or in solid zinc structures, is preferred in that it can be recycled and reused. Therefore, the materials used in the obstacles are reusable. In addition, many of the captured contaminants, especially heavy metals such as mercury, are reusable for lighting and chlorine production.

Referring to FIG. 16, another exemplary reverse venturi device 15 is shown in which the expanded diameter chamber 45 has a significantly larger volume compared to the volumes of the inlet conduit 43 and outlet conduit 44 . This enlarged diameter portion 46 may be circular, square, triangular, elliptical, or virtually any of a number of shapes desired to provide an enlarged tortuous flow path 77 for the gaseous discharge flowing through the enlarged diameter portion 46 . (a rectangular shape is shown).

Referring to FIG. 17, a block diagram of a typical gas emission control system is shown. Gaseous effluent is introduced from the furnace 47 into an electrostatic precipitator (ESP) 48, a fluidized gas desulfurization (FGD) unit 49, and a fiber filter (FF) unit 50 before being discharged to the atmosphere via a chimney 51. be done. A first concentration of contaminants 52 is removed from the gaseous effluent at ESP 48 . Similarly, a second concentration of contaminants 53 is removed from the gaseous effluent in the FGD unit 49 . The second concentrate 53 produced by the FGD unit 49 often contains mercury and other heavy metals and typically flows into the wastewater. A third concentration of contaminants 54 is removed from the gaseous effluent in the FF unit 50 .

18A and 18B, the block diagram of FIG. 17 is modified in that sorbent injection points are introduced and an additional step is provided in which the gaseous effluent passes through the reverse venturi device 15 described above. there is In FIG. 18A a first sorbent introduction point 55 is shown between furnace 47 and ESP 48 . Alternatively, in FIG. 18B a second sorbent introduction point 56 is shown between the FGD unit 49 and the FF unit 50 . Which option is considered the most favorable for the adsorbent depends on the existing structure and plant conditions. There are many introduction points or combinations of introduction points at which adsorbents can be introduced other than the two options shown in FIGS. 18A and 18B, and thus these two options are shown for illustrative purposes. The reverse venturi device 15 in FIGS. 18A and 18B is arranged after the FF unit 50 and before the chimney 51 . The reverse venturi device 15 may be constructed according to any of the examples described above as suitable for a variety of applications. Ultimately, the final gaseous emissions exiting the reverse venturi device 15 and released into the atmosphere through the chimney 51 will be able to meet and exceed current and future EPA emissions rules and regulations.

The method illustrated in FIGS. 18A and 18B burns fuel in a furnace 47 to generate a pollutant-laden gaseous effluent, flows the gaseous effluent from the furnace 47 into an ESP 48, and uses the ESP 48 to exhaust the gaseous effluent. a step of removing first part particulate contaminants in the article; Using ESP 48 to remove a first portion of the particulate contaminants in the gaseous effluent forms a first concentrate 52 that includes a first portion of the particulate contaminants removed from the gaseous effluent by ESP 48 . In operation, the ESP 48 uses an applied electrostatic charge to remove fine contaminants from the gas exhaust. The method also includes introducing the gaseous effluent from ESP 48 to FGD unit 49 and using FGD unit 49 to remove sulfur dioxide contaminants in the gaseous effluent. The step of removing sulfur dioxide contaminants in the gaseous effluent using the FGD unit 49 forms a second concentrate 53 comprising the sulfur dioxide contaminants removed from the gaseous effluent by the FGD unit 49 . The method further comprises introducing the gaseous effluent from the FGD unit 49 to an FF unit 50 (i.e., baghouse) and using the FF unit 50 to remove a second portion of the particulate contaminants in the gaseous effluent. including. A third enrichment comprising a second portion of the particulate contaminants removed from the gaseous effluent by the FF unit 50 by removing the second portion of the particulate contaminants in the gaseous effluent using the FF unit 50 An object 54 is formed. In operation, contaminant particles are removed from the gas effluent as it passes through one or more fiber filters (not shown) of the FF unit 50 .

In accordance with the present disclosure, the method further includes the steps of directing the gaseous effluent from the FF unit 50 to a reverse venturi device 15 and using the reverse venturi device 15 to remove heavy metal contaminants in the gaseous effluent. The process of removing heavy metal contaminants in the gaseous effluent using the reverse venturi device 15 causes the gaseous effluent to pass through (ie, flow over) a reactant mass disposed within the reverse venturi device 15 . Amalgam-forming metals within the reactant mass chemically combine with heavy metal contaminants in the gaseous effluent. Thus, the heavy metal contaminants in the reverse venturi device 15 are captured by the reactant mass as they combine with the amalgam-forming metals in the reactant mass. The method also passes the gaseous effluent from the reverse venturi device 15 to a chimney 51 which discharges the gaseous effluent to the surrounding atmosphere. The reverse venturi device 15 has a relatively small footprint and can easily be installed harmoniously between the existing system emission control devices 48, 49, 50 and the chimney 51 to the atmosphere. It is advantageous in terms of

The method may include injecting the sorbent into the gaseous effluent. According to this process, sorbent may be injected into the gaseous effluent at a first sorbent introduction point 55 located between furnace 47 and ESP 48, as shown in FIG. 18A. Alternatively, the sorbent may be injected into the gaseous effluent at a second sorbent introduction point 56 located between the FGD unit 49 and the FF unit 50, as shown in FIG. 18B. The adsorbent includes an amalgam-forming metal and binds at least a portion of the heavy metal contaminants in the gaseous effluent before the gaseous effluent enters the reverse venturi device 15 . By injecting the sorbent into the gaseous effluent at either the first sorbent introduction point 55 or the second sorbent introduction point 56, more mercury, heavy metals and acid gases are released at previously unrealizable levels. It can be collected in the FF unit 50. As mentioned above, the amalgam-forming metal may be selected from the group consisting of zinc, iron and aluminum, and the adsorbent may for example be a CZTS compound. The sorbent can be regenerated and activated so that hazardous pollutants can be collected and recycled.

Referring to FIG. 19, a block diagram of a typical non-gaseous emissions control system is shown. Liquid and/or liquid-like effluent is passed from the fluidized gas desulfurization (FGD) unit 59 and/or from the wet gas scrubbing unit 58 to the lime treatment unit 60 before being sent to the settling tank 61 . After a suitable period of time, this non-gaseous effluent is passed from the settling tank 61 into a pretreatment system or dewatering system 62 for dry waste 64 . Non-gaseous effluents sent through the process of dry waste 64 are prepared for disposal in landfill 65 . The non-gaseous effluent sent through a dewatering system 62, optionally comprising a recirculation system, is prepared for use within a secondary industrial process 63, which may include, for example, gypsum and/or cement production. Non-gaseous effluents from settling basin 61 that are not directed to treatment for dewatering system 62 or dry waste 64 are directed to discharge through drain 66 . The final non-gaseous emissions discharged into this drain 66 are not as regulated as they may be in the years to come. The proposed EPA water effluent rules and regulations are extremely restrictive compared to the effluents that can currently be discharged into drains. Industries that need to discharge contaminated liquid effluents into drains have current effluent control technology that has virtually no chance of meeting and/or complying with upcoming EPA regulations.

Referring to Figure 20, the block diagram of Figure 19 is modified by one or more treatment vessels 67 containing the adsorbents described above. After the non-gaseous effluents are sent from the sedimentation tank 61 and before they are discharged into a drain 66, a treatment tank 67 is placed. The method illustrated in FIG. 20 collects pollutant-laden non-gaseous effluent and passes the non-gaseous effluent through FGD unit 59 and/or wet scrubber 58 to remove some of the contaminants in the non-gaseous effluent. The non-gaseous effluent from the FGD unit 59 and/or the wet scrubber 58 is sent to a lime treatment unit 60, and the non-gaseous effluent is passed through the lime treatment unit 60 to be processed by the Clark process. A step of softening the non-gaseous effluent is included. In operation, lime processing unit 60 removes certain ions (eg, calcium (Ca) and magnesium (Mg)) from the non-gaseous effluent by precipitation. This method sends the non-gaseous effluent from the lime processing unit 60 to a sedimentation basin 61 to settle out and remove a portion of the contaminants in the non-gaseous effluent, and the non-gaseous effluent in the sedimentation basin 61 to dewatering a portion and using the dewatered by-product in a secondary industrial process 63 to remove a second portion of the non-gaseous effluent from the sedimentation basin 61 to dry waste a second portion of this non-gaseous effluent; 64 is also included. In the step of dewatering a first portion of the non-gaseous effluent in the settling tank and utilizing the dehydrated by-product in a secondary industrial process 63, the dewatering step includes recycling the first portion of the non-gaseous effluent. Alternatively, secondary industrial processes 63 may include, for example, gypsum or cement manufacturing processes. In the step of removing a second portion of the non-gaseous effluent from the settling basin 61 and applying a dry waste treatment 64 to the second portion of the non-gaseous effluent, the dry waste treatment 64 is the second portion of the non-gaseous effluent. in a waste dump 65.

In the present disclosure, the method further includes the step of passing a third portion of the non-gaseous effluent in settling tank 61 to treatment tank 67 containing the disclosed adsorbents. The sorbent contains amalgam-forming metals that bind heavy metal contaminants in the non-gaseous effluent. The sorbent thus captures heavy metal contaminants in treatment vessel 67 as they bind to the sorbent and precipitate/precipitate out of the non-gaseous effluent. The method may then direct the non-gaseous effluent from treatment tank 67 to drain 66 for discharge. Treatment vessel 67 may be designed to allow non-gaseous effluent (ie, wastewater stream) to flow out of treatment vessel 67 continuously.

Several exemplary embodiments are disclosed for the sorbents disclosed herein. These illustrative embodiments are merely examples and are not meant to represent an exhaustive list of possible variations on this theme.

As noted above, one exemplary sorbent is elemental zinc powder. The zinc powder consists of elemental zinc. Zinc can be used as a powder or as granules. One method used to extend the useful life and reduce and/or prevent pre-oxidation of zinc powder and/or granules used in any gaseous emissions at high temperatures is to is mixed with or coated with solid acids such as sulfamic acid, citric acid and other organic acids. This powder/acid mixture may be injected into the gaseous effluent (eg, flue gas stream) and/or placed in a suitable embodiment of the reverse venturi device 15 .

The optimum particle size for zinc powder ranges from 0.5 nanometers to 7,500 microns. In addition, powder mixtures having different size particle size ranges have been found to be advantageous, particularly when the particle size range is from 0.5 nanometers to 7,500 microns. Similarly, the optimum particle size for zinc granules ranges from 7,500 microns to 3.0 inches. In addition, mixtures of granules having different size particle size ranges have been found to be advantageous, particularly when the particle size range is from 7,500 microns to 3.0 inches.

In another exemplary embodiment, the adsorbent is CZTS with the molecular formula Cu2ZnSnS4. The CZTS may also consist of other phases of copper, zinc, tin and sulfur, which is also advantageous. The CZTS and/or related phases copper, zinc, tin and sulfur may be mixed in stoichiometric proportions followed by mechanochemical compounding in a mill. Additionally, the CZTS may be mixed with either clay, such as bentonite or zeolite, and calcium hydroxide (CaOH) in equal proportions. The optimum particle size for CZTS powder ranges from 0.5 nanometers to 7,500 microns. During testing and development, CZTS powder mixtures with different size particle size ranges have been found to be advantageous, especially when the particle size range is from 0.5 nanometers to 7,500 microns. For applications where special CZTS granules are preferred, the optimum particle size has been found to range from 7500 microns to 3.0 inches. Additionally, mixtures of CZTS granules having different size particle size ranges have been found to be advantageous, particularly when the particle size range is from 7,500 microns to 3.0 inches.

For most contaminants, CZTS is most efficient at the smallest particle size within the range mentioned above and when metallic phase CZTS is present in abundance. Note that copper, zinc, tin, and sulfur are not completely converted to CZTS during the production of CZTS, resulting in a mixture of phases (eg, dambalite (CuZn2) and tin sulfide (SnS)).

In one exemplary method of manufacturing CZTS, copper, zinc, tin, and sulfur are added to the grinder in no particular order. The comminution step is accomplished using a ball mill or some type of attrition comminutor, or a combination of comminution devices used sequentially to obtain the desired particle size. Exemplary particle sizes range from a 325 standard mesh screen to a 100 standard mesh screen (1 standard mesh screen = 7500 microns). The resulting particles are further weighed to a predetermined molar ratio of copper:zinc:tin:sulfur=1.7:1.2:1.0:4.0. After confirming the mesh size and molar ratio, these particles are milled and mechanochemically compounded into CZTS and other phases. Grinding time is controlled for optimum properties depending on the specific application. The pulverization process may be a wet pulverization process in which a suitable solvent such as glycol ether, ethylene glycol, ammonia or other alcohol is added, which is carried out in an inert gas atmosphere, or a dry pulverization process which is carried out in an inert gas atmosphere. can be performed using

During the milling process, intermittent sampling is performed to determine the particle size using a particle size analyzer, SEM, XRD, or to determine the phase transformation ratio using the Raman method. The ball size of the grinder is important and tests have shown that it is optimized when the ball-to-powder weight ratio (charge ratio) is at least 5:1. . The grinding balls are most preferably made of steel, ceramics, zirconia or other material that achieves size and/or phase transformations without contaminating the final product. If wet milling is employed, the CZTS is dried. The CZTS is then mixed using a ribbon blender, V-blender or other suitable mixer to evenly mix the bentonite or zeolite and calcium hydroxide.

According to the method described above, the adsorbent is introduced into the gaseous effluent at a temperature of approximately 750° F. or less. The adsorbent is introduced into the gaseous effluent by any of several methods including, but not limited to, injection, fluidized bed, coated filters and trapping. Installation methods can be selected for ease of installation based on existing emission control systems in the plant. One convenient method is to inject CZTS into the gaseous effluent instead of activated carbon, and the same injection equipment can be used with or without modification.

In some applications, gaseous emissions treatment is optimized when CZTS is mixed with bentonite for effective contaminant removal. Alternatively, treatment of non-gaseous emissions is optimized when CZTS is mixed with zeolites. In addition to the specific materials mixed with the CZTS, the ratio of the mixture may be application specific to provide optimum contaminant removal capabilities.

As shown in FIGS. 18A and 18B, when CZTS is used for gaseous effluent treatment, a fiber filter unit 50 is positioned downstream of the CZTS introduction points 55, 56 so that the sorbent particles are captured by the fiber filter unit 50. , to increase the contact time between the gaseous effluent and the adsorbent. Depositing the sorbent on the fiber filters (or bags) of the fiber filter unit 50 allows for longer contact between the gaseous effluent and the sorbent, and allows the sorbent to be collected for subsequent regeneration. can be done. The small particle size of the sorbent allows it to be channeled along the flow of the gaseous effluent much like dust is carried by the wind. During the period in which the adsorbent is entrained in the gaseous effluent stream, the adsorbent contacts contaminants moving in the gaseous effluent stream, thereby causing the contaminants to chemically react and bond with the adsorbent. become. Upon reaching the fiber filter unit 50, while the gaseous effluent continues to pass through the filters in the fiber filter unit 50, the combined adsorbent and contaminant particles are too large to pass through the filter. If the CZTS particles are 10 microns or less, the filter in the fiber filter unit 50 may be pre-coated with larger CZTS particles, activated carbon, talc, lime or other suitable material to prevent the smaller CZTS particles from passing through the filter. may need to. Alternatively, smaller micron size filters may be used in the fiber filter unit 50 .

In other applications for non-gaseous emissions, the CZTS may be introduced into treatment vessel 67 shown in FIG. In this configuration, the CZTS is preferably introduced into the treatment vessel 67 and well agitated for a period of time, after which the non-gaseous effluent (eg, wastewater) undergoes pH adjustment, flocculation, and filtration prior to discharge. The CZTS in treatment bath 67 may then be subjected to a regeneration step to remove contaminants from the CZTS. Spent CZTS can be regenerated by filtering the mercury from the CZTS or by vacuum distillation. The resulting contaminants can then be used in other industries. CZTS also provides the advantage of being able to reduce nitrate and nitride levels in the non-gaseous effluent.

Effluent regulations set by the EPA and coming into effect in 2016 are much stricter than those for air. Some of the current EPA regulations listed in units of nanograms/liter (ng/L), micrograms/liter (μg/L), and/or grams/L are: Arsenic (As) 8 μg/l; Selenium (Se) 10 μg/l; Nitrogen dioxide (NO2) and nitrates (NO3) 0.13 g/l. Other heavy metals such as lead (Pb) and cadmium (Cd) are also included in the proposed EPA control levels. In many existing plants, wastewater with pollution levels exceeding acceptable discharge regulations is sent to a reservoir and/or some other type of sludge reservoir. A CZTS can treat solids in a water reservoir in the same way it treats non-gaseous effluents disclosed herein. Depending on the ionic form of the heavy metals, sludge composition and/or pH, the contact time in the CZTS reservoir can be adjusted appropriately. Sufficient pH adjustment, flocculation, and subsequent filtration allow for normal discharge, disposal, and/or other industrial uses, none of which were previously possible.

It should be noted that the sorbents disclosed herein do not contain any free carbon, including activated carbon currently used in the industry. As a result, none of the metal sulfides produced as a by-product of the disclosed method are filtered. These by-products are therefore of high industrial value in gypsum wallboard and cement applications. EPA's metal sulfide filtration tests are well known and well documented for use in these products.

Activated carbon is available in some alternative configurations, but these variations limit the use of activated carbon so that it cannot leak into the effluent. For example, in one example activated carbon is embedded in the filter of the fiber filter unit 50 . This activated carbon does not leak freely into the gaseous effluent stream. As another limited use of activated carbon, it is possible to coat CZTS in crystalline form with activated carbon to produce CZTS with a carbon film thickness of 1.0 nanometers or less. This facilitates the capture of very small mercury metal vapor particles. Similarly, crystalline CZTS can be coated with nanometric zeolite films or other coatings to target specific hazardous contaminants for specific applications. Again, the activated carbon in this example is not free to leak into the gaseous effluent stream. In another configuration shown in FIG. 33, an inverted venturi fluidized bed apparatus washes the adsorbent as a series of adsorbent recycling subsystems for CZTS adsorbents, CZTS alloy adsorbents, and/or carbon-based adsorbents. Equipped with facilities for recycling.

Referring to FIG. 21, a graph illustrates the percentage of contaminants removed from emissions by known emission control systems and the percentage of contaminants removed by the reverse venturi device and method disclosed herein. . The EPA currently mandates a 90% pollutant level 78 for gaseous emissions. Existing emission control systems 79 are effective in removing 88% to 90% of hazardous pollutants. However, the EPA has increased the required minimum pollutant removal rate over the years, and many existing emission control systems are unable to meet this requirement, and many other existing emission control systems are: Requirements can only be met when operating at the maximum removal capacity available under current technology.

Still referring to FIG. 21 , an exemplary emission control system 80 is a novel emission control system based on the reverse venturi device, sorbents and/or methods disclosed herein, or the emissions control system disclosed herein. It can be any existing emission control system modified and enhanced to include a reverse venturi device, sorbent and/or method. Testing has confirmed that this exemplary emission control system 80 is capable and effective in removing at least 98% of hazardous pollutants, well above current EPA regulatory levels.

22 and 24, a pollutant gas source 150 is introduced into the system through one or more pre-fluidized bed filters 151, a fluidized bed 152, one or more post-fluidized filters Through floor filter 153, system exhaust 154, and exhaust gas emissions through chimney 155 in an environmentally controlled manner. It should be noted that it is not necessary to first pass the contaminated gas source 150 through one or more pre-fluidized bed filters 151 . However, more than one pre-fluidized bed filter 151 may be required depending on the particular application.

The fluidized bed 152 has an inverted venturi geometry with a specific length L to diameter D ratio of 2.9:1 minimum and 9.8:1 maximum. This ratio is optimized for longer residence time of the pollutant gas source 150 in the fluidized bed 152 packed with the specialized adsorbent, such as the reactant 164 . Reactant 164 is an adsorbent comprising copper, zinc, tin, sulfur (CZTS) compounds and/or alloys thereof. An example of a preferred ratio of length L to diameter D of fluidized bed 152 is 4.4:1, which is determined through trial and error.

Preferably, fluidized bed 152 has a generally circular cross-section. Although not shown in FIG. 24, fluidized bed 152 may include one or more of the various baffles and/or other application-specific flow restricting obstructions disclosed herein. Fluidized bed 152 has generally outwardly extending convex ends 168 and 169 to facilitate extended residence time while minimizing turbulence through reactant 164 . As the flow of pollutant gas source 150 enters fluidized bed 152 at inlet holes 165 , it begins to come into intimate contact with reactant 164 resulting in random, non-turbulent flow 166 . Random non-turbulent flow 166 is reversed on its own side by generally outwardly extending convex ends 168 and 169 , thereby causing unturbulent flow 166 to flow within fluidized bed 152 before exiting fluidized bed 152 through exit holes 167 . Extended residence time. The reactant 164 that promotes non-turbulent flow 166 forms a random tortuous flow path of the pollutant gas source 150 . Note that the length L of fluidized bed 152 does not include the length of convex ends 168 and 169 .

The fluidized bed 152 has side bleed holes 170 leading to the sorbent wash station 156 . A sorbent wash station 156 can remove spent sorbent 157 from the system for disposal. Additionally, the contaminants 158 captured from the contaminant gas source 150 by the reactants 164 and separated from the reactants 164 at the adsorbent wash station 156 can be disposed of and/or recycled. Adsorbent wash station 156 returns washed reactant 164 to fluidized bed 152 via adsorbent return port 159 . A bulk refill sorbent vessel 168 provides replenishment of reactant 164 to replace depleted sorbent 157 as needed. A system exhaust 154 provides gaseous effluent that is discharged in an environmentally controlled manner through an exhaust stack 155 . Additional sorbent recycling subsystems (FIG. 33) may be provided to further discharge trapped waste 160 .

23 and 24, a contaminated non-gas source 161 is introduced into the system through one or more pre-fluidized bed filters 151, a fluidized bed 152, one or more post Non-gaseous effluents are discharged by environmentally controlled discharge 162 through fluidized bed filter 153 via system discharge 154 . Note that it is not necessary to first pass the contaminated non-gas source 161 through one or more pre-fluidized bed filters 151 . However, more than one pre-fluidized bed filter 151 may be required depending on the particular application.

The fluidized bed 152 has an inverted venturi geometry with a specific length L to diameter D ratio of 2.9:1 minimum and 9.8:1 maximum. This ratio is optimized for longer residence time of the contaminated non-gas source 161 in the fluidized bed 152 packed with special adsorbents such as reactants 164 . Reactant 164 is an adsorbent comprising copper, zinc, tin, sulfur (CZTS) compounds and/or alloys thereof. An example of a preferred ratio of length L to diameter D of fluidized bed 152 is 4.4:1, which is determined through trial and error.

Fluidized bed 152 preferably has generally outwardly extending convex ends 168 and 169 to facilitate extended residence time while minimizing turbulence through reactant 164 . As the flow of contaminated non-gas source 161 enters fluidized bed 152 at inlet holes 165 , it begins to come into intimate contact with reactant 164 , resulting in random, non-turbulent flow 166 . The random, non-turbulent flow 166 is reversed on its own side by generally outwardly extending convex ends 168 and 169, thereby extending the residence time within the fluidized bed 152 before exiting the fluidized bed 152 through exit holes 167. be. A reactant 164 that promotes non-turbulent flow 166 forms a random tortuous flow path of the polluting non-gas source 161 . Note that the length L of fluidized bed 152 does not include the length of convex ends 168 and 169 .

Preferably, fluidized bed 152 has a generally circular cross-section. Although not shown in FIG. 24, fluidized bed 152 may include one or more of the various baffles and/or application-specific flow-restricting obstructions disclosed herein. The fluidized bed 152 has side bleed holes 170 leading to the sorbent wash station 156 . A sorbent wash station 156 can remove spent sorbent 157 from the system for disposal. Additionally, contaminants 158 captured from contaminated non-gas source 161 by reactant 164 and separated from reactant 164 at adsorbent wash station 156 can be disposed of and/or recycled. Adsorbent wash station 156 returns washed reactant 164 to fluidized bed 152 via adsorbent return port 159 . A bulk refill sorbent vessel 168 provides replenishment of reactant 164 to replace depleted sorbent 157 as needed. System exhaust 154 provides non-gaseous emissions that are expelled by environmentally controlled release 162 . An additional discharge for trapped waste 163 is also provided.

FIG. 25 passes gaseous emissions 250 through one or more pre-filters 251, fluidized bed 253, one or more post-filters 255, system exhaust 256, and ultimately through exhaust stack 257 and/or the exhaust An exemplary method of venting as a controlled vented gaseous effluent through disposal process 262 is shown. Fluidized bed 253 is bisected by longitudinal surface 290 . Inlet P3 and outlet P4 are configured to allow gaseous effluent to enter and exit when fluidized bed 253 is aligned with longitudinal surface 290 . Obstructions (not shown) within the fluidized bed 253 form a preferred tortuous flow path that is particularly suitable for gaseous effluent entering through inlet hole P3 and exiting through outlet hole P4. be done. The inlet hole P3 and the outlet hole P4 are arranged above the longitudinal surface 290 of the fluidized bed 253 .

As shown in FIG. 25, fluidized bed 253 is mountable on track 254 and is configured to tilt fluidized bed 253 about axis of rotation 252 . As the gaseous effluent is processed in the fluidized bed 253, the longitudinal surface 290 of the fluidized bed 253 is generally horizontal. An adsorbent wash station 258 communicates with the outlet P5 of the fluidized bed 253 where contaminant particles captured by the adsorbent are removed. The removed contaminants can be recycled by station 261 or discarded. The spent adsorbent is discarded by station 259 and the washed adsorbent is recycled from adsorbent return port 260 back to fluidized bed 253 through return port P6.

26, contaminated non-gaseous effluent 295 is passed through one or more pre-filters 251, fluidized bed 253, one or more post-filters 255, system exhaust 256, and finally an environmentally controlled Exemplary methods of exhausting as non-gaseous emissions 273 and/or via an emissions disposal process 274 are shown. The inlet P2 and outlet P1 are configured to allow non-gaseous effluent to enter and exit. Obstructions (not shown) within fluidized bed 253 provide a suitable tortuous flow path that is particularly suitable for introducing non-gaseous effluent through inlet P2 and outlet P1. The inlet hole P2 and the outlet hole P1 are bisected by a longitudinal surface 290 of the fluidized bed 253 (ie aligned with the longitudinal surface 290 of the fluidized bed 253).

When the non-gaseous effluent is processed in fluidized bed 253, longitudinal surface 290 of fluidized bed 253 is generally vertical. An adsorbent wash station 258 communicates with the outlet P5 of the fluidized bed 253 where contaminant particles captured by the adsorbent are removed. The removed contaminants can be recycled by station 261 or discarded. The spent adsorbent is discarded by station 259 and the washed adsorbent is recycled from adsorbent return port 260 back to fluidized bed 253 through return port P6.

A table comparing the disclosed preferred reactive CZTS alloy sorbent 341 with other sorbents including activated carbon 342 and zeolite 343 is shown in FIG. Contaminants 367 include major classes including nitrogen 368, phosphorus 369, heavy metals 370, sulfur 371, mercury 372, and selenate 373. Contaminants 367 are further listed with each adsorbent tabulating gaseous emissions 344 , 346 , and 348 compared to non-gas emissions 345 , 347 , and 349 .

Testing confirms that reactive CZTS alloy sorbent 341 is effective in capturing and removing contaminants 367 in gaseous effluent 344 and/or non-gaseous effluent 345 . In contrast, activated carbon 342 is not effective in capturing and removing contaminants 367 in gaseous effluent 346 and/or non-gaseous effluent 347 . Similarly, zeolite 343 is not effective in capturing and removing contaminants 367 in gaseous effluent 348 and/or non-gaseous effluent 349 .

FIG. 28 shows an expanded list of adsorbents including reactive CZTS alloy adsorbents 351 and other adsorbents including corrosive agents 350, ferric oxide 355, and zeolites 356 of the present disclosure. Reactive CZTS alloy adsorbents 351 include CZTS sulfur alloy 352, CZTS selenate alloy 353, and ferrous oxide CZTS alloy 354. CZTS alloy sorbent 351 effectively reacts with all of the following contaminant groups. selenate 357, fully ionized sulfur 358, fully ionized nitrogen 359, and fully ionized phosphorus 360. Reactive CZTS alloy sorbent 351 is capable of capturing and removing these contaminants from both gaseous and non-gaseous effluents.

In contrast, corrosive agent 350 is effective only against fully ionized sulfur 358 . Ferric oxide 355 is effective only with selenate 357 and has very slow reaction properties (and acts only on non-gaseous emissions) with fully nitrogen 359 and fully ionized phosphorus 360. . Zeolite 356 is only effective against fully ionized nitrogen 359 and fully ionized phosphorus 360 . Thus, known adsorbents such as corrosives 350, ferric oxide 355, and zeolite 356 have limited effectiveness characteristics compared to the broad range of reactive CZTS alloy adsorbents 351 disclosed herein. have Even if known sorbents have a certain level of effectiveness, they are all below the effective level of the reactive CZTS alloy sorbent 351 disclosed herein.

In FIG. 29, Table 364 shows post-treatment after use in an emissions control system that captures and removes contaminants 367 including nitrogen 368, phosphorus 369, heavy metals 370, sulfur 371, mercury 372, and selenate 373. 3 shows the ability of the prior art sorbent 365 to The ability to separate contaminants 367 from prior art sorbents in gaseous effluent 374 and/or non-gaseous effluent 375 is very low and virtually nonexistent except for nitrogen 368 in gaseous effluent 374 . Similarly, table 364 shows that the reusability of prior art adsorbent 366 after separation of contaminants 367 is also virtually non-existent, with the exception of gaseous effluent 376 containing nitrogen 368 .

In FIG. 30, Table 378 shows post-treatment after use in an emissions control system that captures and removes contaminants 367 including nitrogen 368, phosphorus 369, heavy metals 370, sulfur 371, mercury 372, and selenate 373. shows the ability of the reactive CZTS alloy sorbent 339 disclosed herein to It is particularly advantageous to be able to separate contaminants 367 in gaseous effluent 374 and/or non-gaseous effluent 375 from the disclosed reactive CZTS alloy sorbent 339 . Because this means that contaminants 367 can be more easily disposed of or recycled, and because reactive CZTS alloy sorbent 339 can be reused in emission control systems (shown in Table 378). is. Specifically, Table 378 shows that the reactive CZTS alloy sorbent 340 disclosed herein can be reused after being separated from contaminants 367 in gaseous effluent 376 and non-gaseous effluent 377 .

In FIG. 31, a block diagram illustrates a system and method for removing contaminants from gaseous exhaust 250. In FIG. The gaseous emissions 250 are monitored and analyzed at step 379 to determine the types and levels of contaminants in the gaseous emissions 250 . Monitoring can be systematic intermittent sampling at regular intervals, or continuous in-line monitoring and analysis. Based on the type and/or level of contaminants present in the gaseous effluent 250 as determined by step 379, the effluent flow may be directed to the appropriate prefilters 381, 382, 383, and/or 384 where the gaseous effluent 250 is filtered. through the pre-filter inlet manifold 380 so as to be further directed to . Appropriate pre-filters 381, 382, 383 and/or 384 are selected by the selection method shown in FIG.

The pre-filter shown in FIG. 31 is filled with reactive CZTS alloy adsorbent 351 shown in FIG. For example, the pre-filter 381 is filled with sulfur CZTS alloy 352 shown in FIG. The prefilter 382 is filled with selenate CZTS alloy 353 shown in FIG. The prefilter 383 is filled with ferrous oxide CZTS alloy 354 shown in FIG. Pre-filter 384 is filled with a combination of CZTS alloy adsorbents 352, 353 and/or 354. Additions filled with different combinations of CZTS alloy sorbents 352, 353, and/or 354, each combined to effectively treat specific levels and/or types of contaminants contained in gaseous effluent 250. of pre-filters may be added to pre-filter inlet manifold 380 .

After the contaminated gaseous effluent 250 is routed to the appropriate prefilters, prefilter effluent manifold 385 directs the effluent to fluidized bed 253 . For gaseous exhaust 250 , the enclosure of fluidized bed 253 is oriented substantially parallel to pedestal 271 . Contaminants are separated from the adsorbent in step 258 and returned to fluidized bed 253 through adsorbent return port 260 .

After the gas effluent 250 exits the fluidized bed 253 , a post-filter monitoring step 386 determines new levels and/or types of contaminants remaining in the gas effluent 250 and the gas effluent 250 is transferred to the post-filter inlet manifold 387 . led to. Appropriate post-filters 388, 389, 390 and/or 391 are selected by the selection method shown in FIG. The post filter shown in FIG. 31 is filled with reactive CZTS alloy adsorbent 351 shown in FIG. For example, post filter 388 is filled with sulfur CZTS alloy 352 shown in FIG. The post filter 389 is filled with selenate CZTS alloy 353 shown in FIG. The post filter 390 is filled with ferrous oxide CZTS alloy 354 shown in FIG. Post filter 391 is filled with a combination of CZTS alloy adsorbents 352, 353 and/or 354. Post-filter outlet manifold 392 directs gaseous exhaust 250 to gas system exhaust 256a. At the gas system discharge 256a, a portion of the gas effluent 250 is discharged through a controlled gas discharge chimney 257 and a portion of the gas effluent 250 is discharged through a suitable waste treatment process 262.

Additions filled with different combinations of CZTS alloy sorbents 352, 353, and/or 354, each combined to effectively treat specific levels and/or types of contaminants contained in gaseous effluent 250. of post-filters may be added to post-filter inlet manifold 387 .

All pre-filters 381 , 382 , 383 , 384 and post-filters 388 , 389 , 390 , 391 are fed separately via sorbent wash step 258 and sorbent return port 260 . Step 258 includes separating the contaminants from the CZTS alloy sorbent 351 and recycling and/or appropriately recovering the contaminants for disposal 261 . Any spent CZTS alloy sorbent 351 can be disposed of via disposal step 259 . After step 258, the specific CZTS alloy adsorbent 351 may be replaced with each specific pre-filter 381, 382, 383, 384 and/or post-filter 388, 389, 390, 391. a specific routing diagram and/or for routing the adsorbent from the adsorbent wash step 258 and from the pre-filters 381, 382, 383, 384 and/or post-filters 388, 389, 390, 391 to the adsorbent wash step 258; A schematic is not shown.

In FIG. 32, a block diagram illustrates a system and method for removing contaminants from non-gaseous emissions 295 . The non-gaseous effluent 295 is monitored and analyzed at step 379 to determine the types and levels of contaminants in the non-gaseous effluent 295 . Monitoring can be systematic intermittent sampling at regular intervals and/or continuous in-line monitoring and analysis. Based on the type and/or level of contaminants present in the non-gaseous effluent 295 as determined by step 379, the flow of effluent may be directed through the appropriate pre-filters 381, 382, 383, and/or the non-gaseous effluent 295. or through pre-filter inlet manifold 380 to be further directed to 384 . Appropriate pre-filters 381, 382, 383 and/or 384 are selected by the selection method shown in FIG.

The prefilter shown in FIG. 32 is filled with a reactive CZTS alloy adsorbent shown in FIG. For example, the pre-filter 381 is filled with sulfur CZTS alloy 352 shown in FIG. The prefilter 382 is filled with selenate CZTS alloy 353 shown in FIG. The prefilter 383 is filled with ferrous oxide CZTS alloy 354 shown in FIG. Pre-filter 384 is filled with a combination of CZTS alloy adsorbents 352, 353 and/or 354. Loaded with different combinations of CZTS alloy sorbents 352, 353, and/or 354, each combined to effectively treat specific levels and/or types of contaminants contained in non-gaseous effluent 295 Additional pre-filters may be added to pre-filter inlet manifold 380 .

After the contaminated non-gaseous effluent 295 is routed to the appropriate prefilters, the prefilter effluent manifold 385 directs the effluent to the fluidized bed 253 . For non-gaseous effluent 295 , the enclosure of fluidized bed 253 is oriented substantially perpendicular to pedestal 271 . Contaminants are separated from the adsorbent in step 258 and returned to fluidized bed 253 through adsorbent return port 260 .

After the non-gaseous effluent 295 exits the fluidized bed 253, a post-filter monitoring step 386 determines the new level and/or type of contaminants remaining in the non-gaseous effluent 295, and the non-gaseous effluent 295 is post-filtered. It is sent through the inflow manifold 387 . Appropriate post-filters 388, 389, 390 and/or 391 are selected by the selection method shown in FIG. The post filter shown in FIG. 32 is filled with reactive CZTS alloy adsorbent 351 shown in FIG. For example, post filter 388 is filled with sulfur CZTS alloy 352 shown in FIG. The post filter 389 is filled with selenate CZTS alloy 353 shown in FIG. The post filter 390 is filled with ferrous oxide CZTS alloy 354 shown in FIG. A post filter 391 is filled with a combination of CZTS alloy adsorbents 352, 353 and/or 354. Post-filter effluent manifold 392 directs non-gaseous exhaust 295 to non-gaseous system exhaust 256b. At the non-gaseous system exhaust 256b, a portion of the non-gaseous effluent 295 is exhausted as an environmentally controlled non-gaseous exhaust 273, and a portion of the non-gaseous effluent 295 is exhausted by a suitable waste treatment process 262. be. Loaded with different combinations of CZTS alloy sorbents 352, 353, and/or 354, each combined to effectively treat specific levels and/or types of contaminants contained in non-gaseous effluent 295 Additional post-filters may be added to post-filter inlet manifold 387 .

All pre-filters 381 , 382 , 383 , 384 and post-filters 388 , 389 , 390 , 391 are fed separately via sorbent wash step 258 and sorbent return port 260 . Step 258 includes separating the contaminants from the CZTS alloy sorbent 351 and recycling and/or appropriately recovering the contaminants for disposal 261 . Any spent CZTS alloy sorbent 351 can be disposed of via disposal step 259 . After step 258, the specific CZTS alloy adsorbent 351 may be replaced with each specific pre-filter 381, 382, 383, 384 and/or post-filter 388, 389, 390, 391. a specific routing diagram and/or for routing adsorbent from the adsorbent wash step 258 and from the pre-filters 388, 389, 390, 391 and/or post-filters 388, 389, 390, 391 to the adsorbent wash step 258; A schematic is not shown.

An exemplary emissions control system is shown in FIG. Contaminated effluent is introduced into fluidized bed 152 via inlet 165 . Note that the effluent may first pass through one or more pre-fluidized bed filters 151 (FIGS. 22 and 23), depending on the needs of a particular application.

The fluidized bed 152 has a housing 16 with an inverted venturi shape, with a specific length L to diameter D ratio between a minimum of 2.9:1 and a maximum of 9.8:1. . This ratio is optimized for longer residence of contaminated effluent in fluidized bed 152 packed with special reactants 164 containing one or more adsorbents. An example of a preferred ratio of length L to diameter D of fluidized bed 152 is 4.4:1, which is determined through trial and error. One or more exemplary fluidized beds 152 may be connected in series or in parallel, depending on the needs of a particular application.

Preferably, fluidized bed 152 has a generally circular cross-section. Although not shown in FIG. 33, fluidized bed 152 may include one or more of the various baffles and/or application-specific flow-restricting obstructions disclosed herein. Fluidized bed 152 has generally outwardly extending convex ends 168 , 169 to facilitate extended residence time while minimizing turbulence through reactant 164 . As the contaminated effluent flow enters fluidized bed 152 at inlet holes 165 , it initiates intimate contact with reactant 164 and random, non-turbulent flow 166 occurs. Random non-turbulent flow 166 is reversed on its own side by generally outwardly extending convex ends 168 , 169 , thereby causing non-turbulent flow 166 to flow within fluidized bed 152 before exiting fluidized bed 152 through exit holes 167 . Extended residence time. Reactants 164 that promote non-turbulent flow 166 create a random tortuous flow path of contaminated effluent. Note that the length L of the fluidized bed 152 does not include the length of the convex ends 168,169.

Fluidized bed 152 includes at least one monitoring sensor station 421 (ie, first monitoring sensor) that provides data, status and feedback on operating parameters. Monitoring sensor station 421 is configured to monitor exhaust flow levels, pressure, velocity, temperature, and many other relevant parameters for the emissions control system. While some automatic adjustments are made by the device based on feedback information, other process and/or system parameters may require manual adjustments. Monitoring sensor station 421 provides information about the efficiency of the adsorbent within fluidized bed 152 and assists in determining when to wash and/or regenerate the adsorbent.

In an exemplary embodiment of the present disclosure, fluidized bed 152 has at least one side bleed hole 403, 409, 415 leading to adsorbent recycling subsystems 400, 401, 402, respectively. Although the adsorbent recycling subsystems 400 , 401 , 402 shown in FIG. 33 are located outside the fluidized bed 152 , they may alternatively be located inside the fluidized bed 152 .

Fluidized bed 152 includes at least one closed loop adsorbent outlet port monitoring sensor station 422 and at least one closed loop adsorbent return port monitoring sensor station 423 that provides data, status and feedback on operating parameters. Monitoring sensor station 422 is configured to monitor exhaust flow levels, pressure, velocity, temperature, and many other relevant parameters for the emissions control system. While some automatic adjustments are made by the programmable device based on the feedback information, other process and/or system parameters may require manual adjustments. Monitoring sensor 423 identifies the state of the adsorbent as it passes through one of exit holes 403 , 409 or 415 and as it enters subsystem 400 , 401 or 402 . Monitoring sensor station 423 is configured to monitor exhaust flow levels, pressure, velocity, temperature, and many other relevant parameters for the emissions control system.

While some automatic adjustments are made by the programmable device based on the feedback information, other process and/or system parameters may require manual adjustments. Monitoring sensor 423 identifies the state of the adsorbent as it passes through return port 407, 414 or 420 or one of subsystems 400, 401 or 402 after cleaning and/or regeneration. A monitoring sensor station 424 (ie, a second monitoring sensor) is configured to monitor exhaust flow level, pressure, velocity, temperature, and many other relevant parameters for the emissions control system. While some automatic adjustments are made by the programmable device based on the feedback information, other process and/or system parameters may require manual adjustments. Monitoring sensors 424 monitor the state and final state of the adsorbent as it is processed at each station 404, 410, or 416 within subsystems 400, 401, or 402 when cleaning and/or regeneration steps are performed. monitor the volume. Monitoring sensors 421, 422, 423, 424 cooperate with each other to make process conditions and/or parameter adjustments to achieve and maintain consistency and optimal sorbent efficiency at each station in the emissions control system. . Monitoring the sorbent within subsystems 400, 401, 402 determines when and in what amount each station 408, 413, and 419 needs replenishment of sorbent.

In another exemplary embodiment (not shown), a cleaning and/or regeneration subsystem is installed and configured within fluidized bed 152 . In this configuration, the functions of monitoring sensors 421 , 422 , 423 , 424 and adsorbent recycling subsystems 400 , 401 , 402 are performed inside fluidized bed 152 .

In FIG. 33, once the fluidized bed 152 is loaded with the CTZS adsorbent reactant 164, the adsorbent recycling subsystem 400 is used to maintain the CTZS adsorbent in optimum operating conditions. Through sorbent discharge port 403 sorbent can be moved into sorbent recycling station 404 . This adsorbent recycling station 404 within subsystem 400 contains one or more chemical reagents that separate contaminants from the CZTS adsorbent as part of the cleaning and regeneration process. As a non-limiting example, the chemical reagents used within the sorbent recycling station 404 may be selected from the group of fatty alcohols. Spent and/or depleted CZTS sorbent can be disposed of through sorbent disposal station 405 . Effluent contaminants removed from the effluent can be recycled for use in various industries through pollutant waste port 406 . A bulk refill station 408, such as a container of fresh/fresh sorbent, provides replenishment of CZTS sorbent to replace sorbent removed and/or lost during the removal of contaminants from the effluent. be. The closed loop back to fluidized bed 152 is completed at CZTS adsorbent return port 407 .

Once the fluidized bed 152 is loaded with reactants 164 comprising CTZS alloy adsorbents, the adsorbent recycling subsystem 401 maintains the CTZS alloy adsorbents in optimum operating conditions. Through sorbent discharge port 409 sorbent can be moved into sorbent recycling station 410 . This adsorbent recycling station 410 within subsystem 401 contains one or more chemical reagents that separate contaminants from the CZTS alloy adsorbent as part of the cleaning and regeneration process. As a non-limiting example, the chemical reagents used within the sorbent recycling station 410 may be selected from the group of fatty alcohols. Consumed and/or worn CZTS alloy sorbent can be discarded through station 411 . Effluent contaminants removed from the effluent can be recycled for use in various industries through pollutant waste port 412 . A bulk refill station 413 provides a replenishment of CZTS alloy sorbent to replace sorbent removed and/or lost during the removal of contaminants from the effluent. The closed loop back to fluidized bed 152 is completed at CZTS alloy adsorbent return port 414 .

Once the fluidized bed 152 is loaded with the carbon-based adsorbent reactant 164, the adsorbent recycling subsystem 402 maintains the carbon-based adsorbent in optimum operating conditions. Through sorbent discharge port 415 sorbent can be moved into sorbent recycling station 416 . This adsorbent recycling station 416 within subsystem 402 contains one or more chemical reagents that separate contaminants from carbon-based adsorbents as part of the cleaning and regeneration process. By way of non-limiting example, the chemical reagents used within the sorbent recycling station 416 may be solvents such as methyl ethyl ketone, methylene chloride and/or methanol. Consumed and/or depleted carbon-based sorbent can be disposed of through sorbent disposal station 417 . Effluent contaminants removed from the effluent can be recycled for use in various industries through pollutant waste port 418 . A bulk refill station 419 provides a replenishment of carbon-based sorbent to replace sorbent removed and/or lost during the removal of contaminants from the effluent. A carbonaceous adsorbent return port 420 completes the closed loop back to the fluidized bed 152 .

In one exemplary embodiment of the present disclosure, and as shown in FIG. 33, fluidized bed 152 includes one or more adsorbent recycling subsystems 400, 401, 402 configured for one or more adsorbents. may be a single unit with According to another exemplary embodiment (not shown), multiple fluidized beds 152 are configured in series with each other, each fluidized bed 152 configured for one or more adsorbent recycling subsystems 400, 401, 402. . According to another exemplary embodiment (not shown), multiple fluidized beds 152 are configured parallel to each other, each fluidized bed 152 configured for one or more adsorbent recycling subsystems 400, 401, 402. .

Monitoring sensors 421, 422, 423, 424 are but a few non-exhaustive examples of measuring devices applicable to emission control systems. Those skilled in the art will appreciate that there may be many other types of monitoring sensors located at many other emission control system stations not shown in the illustrated embodiment. deaf. The specific monitoring sensors used for gaseous contaminated effluents may differ from the specific monitoring sensors used for non-gaseous contaminated effluents. Similarly, the monitoring sensors required for one type of contaminant may be different than the monitoring sensors required for another contaminant.

In another aspect of the present disclosure, an emission control method for removing pollutants from emissions is disclosed. This method, illustrated in FIG. 33, sends the effluent to a treatment system that includes an inverted venturi fluidized bed apparatus 152 containing one or more adsorbents that chemically bind contaminants contained in the effluent, where the contaminants are adsorbed. After binding to the agent, the step of directing the effluent away from the inverted venturi fluid bed device 152 is included. According to this method, the adsorbent is selected from a group of materials including copper, zinc, tin, sulfur (CZTS) adsorbents, copper, zinc, tin, sulfur (CZTS) alloy adsorbents, and carbon-based adsorbents. be. The method also includes routing the adsorbent through one or more of the adsorbent recycling subsystems 400, 401, 402 for washing and regeneration. This process separates the spent and depleted adsorbent from the adsorbents sent through the adsorbent recycling subsystems 400, 401, 402, discards the depleted and depleted adsorbents, and recycles the adsorbent recycling subsystems 400, 401, 402. separating the contaminants from the adsorbent passed through, discarding or recycling the contaminants, and returning the recycled adsorbent to the reverse venturi fluidized bed apparatus 152 . The method may include sending fresh adsorbent to the reverse venturi fluidized bed apparatus 152 to replace depleted and worn adsorbent.

In embodiments in which the reverse venturi fluidized bed apparatus 152 includes multiple adsorbent recycling subsystems 400, 401, 402, the method further includes retaining different adsorbents within the reverse venturi fluidized bed apparatus 152, One or more monitoring sensors 421, 422, 423, 424 detect at least one process parameter of the reverse venturi fluidized bed apparatus, and based on the at least one process parameter detected by the monitoring sensors 421, 422, 423, 424, one Directing the effluent to these different sorbents may include routing the different sorbents to different sorbent recycling subsystems 400, 401, 402 dedicated to processing specific types of sorbents. For example, in the illustrated embodiment, a copper, zinc, tin, sulfur (CZTS) sorbent is sent through the first sorbent recycling subsystem 400 to produce a copper, zinc, tin, sulfur (CZTS) alloy sorbent. is sent through the second adsorbent recycling subsystem 401 and the carbonaceous adsorbent is sent through the third adsorbent recycling subsystem 402 .

It should be noted that although steps in the method are described and illustrated in a particular order, these steps may vary without departing from the scope of the present disclosure, unless the order of the steps is otherwise stated. They may be performed in order. Similarly, the methods described and illustrated herein can be practiced without all of the above steps, or with additional intermediate steps not described, without departing from the scope of this disclosure. .

The present disclosure is capable of many modifications in light of the above disclosure and can be practiced otherwise than as specifically described within the scope of the appended claims. These preceding statements should be construed to cover any combination in which the inventive novelty would be useful. Use of the word "the" in an apparatus claim indicates an antecedent basis that is positively recited and intended to be included within the scope of the claim, but the word "the" , precede terms that are not intended to be included in the claims.

Claims (20)

An effluent control system comprising a fluidized bed device for removing contaminants from effluent, comprising:
an inlet portion having an inverted venturi shape, into which the discharged matter flows in at a predetermined inlet flow velocity; an outlet portion, through which the discharged matter is discharged at a predetermined outlet flow speed; an enlarged diameter portion that captures the contaminants in the effluent;
the inlet portion, the outlet portion, and the enlarged diameter portion of the housing are in fluid communication with each other;
A reactant mass is disposed within the enlarged diameter portion of the housing, the reactant mass comprising at least copper, zinc, tin, sulfur ( _CZTS ) having the molecular formula _Cu2ZnSnS4 , CZTS alloys, or combinations thereof. having a kind of adsorbent,
the reactant mass has a reactive outer surface positioned in contact with the effluent;
positioned in fluid communication with the housing for receiving sorbent from the housing via a sorbent exhaust port, returning clean sorbent to the housing via a sorbent return port, and at least An emissions control system comprising at least one sorbent recycling subsystem including a chemical reagent for separating said contaminant from a sorbent, said chemical reagent being an aliphatic alcohol. 2. The emission control system of claim 1, wherein the enclosure of the fluidized bed apparatus is permanently installed on-site. 2. The effluent control system of claim 1, wherein said enclosure of said fluidized bed apparatus is transportable. 2. The emissions control system of claim 1, wherein the housing of the fluidized bed apparatus comprises a longitudinal surface oriented generally horizontally when the fluidized bed apparatus is configured for gaseous emissions. Emission control system characterized by: 2. The emissions control system of claim 1, wherein the housing of the fluidized bed apparatus comprises a substantially vertically oriented longitudinal surface when the fluidized bed apparatus is configured for non-gaseous emissions. An emission control system characterized by: 2. The effluent control system of claim 1, wherein said at least one sorbent recycling subsystem is external to said housing of said fluidized bed apparatus. 2. The effluent control system of claim 1, wherein said at least one sorbent recycling subsystem is internal to said housing of said fluidized bed apparatus. 2. The emission control system of claim 1, wherein said at least one sorbent recycling subsystem has a closed loop configuration. 2. The emissions control system of claim 1, wherein said at least one sorbent recycling subsystem includes a sorbent disposal station for separating and discarding exhausted and depleted sorbent. . 2. The effluent control system of claim 1, wherein said at least one sorbent recycling subsystem includes a contaminant waste port for discharging said contaminants separated from said effluent for recycling or disposal. and emission control systems. 2. The emissions control system of claim 1, wherein said at least one sorbent recycling subsystem comprises a bulk refill station supplying fresh sorbent to said sorbent return port to replace depleted and worn sorbent. an emission control system, comprising: 2. The emission control system of claim 1, wherein said at least one sorbent recycling subsystem is configured to process said CZTS. 2. The emission control system of claim 1, wherein the at least one sorbent recycling subsystem is configured to process the CZTS alloy. 2. The emission control system of claim 1, wherein said enlarged diameter portion of said housing further comprises at least one carbon-based sorbent, and said at least one sorbent recycling subsystem comprises said at least one carbon-based sorbent. An emissions control system, characterized in that it is configured to treat a sorbent. 2. The emissions control system of claim 1, wherein the at least one sorbent recycling subsystem comprises:
a first sorbent recycling subsystem connected in fluid communication with the housing of the fluidized bed apparatus at a first sorbent recycling subsystem location and dedicated to processing the CZTS;
a second sorbent recycling subsystem connected in fluid communication with the housing of the fluidized bed apparatus at a second sorbent recycling subsystem location and dedicated to processing the CZTS alloy;
a third sorbent recycling subsystem connected in fluid communication with the housing of the fluidized bed apparatus at a third sorbent recycling subsystem location and dedicated to processing carbon-based sorbents. and emission control systems. 2. The effluent control system of claim 1, further comprising a first monitoring sensor disposed within the enclosure of the fluidized bed apparatus and configured to monitor at least one process parameter of the fluidized bed apparatus. and,
a second monitoring sensor included within said at least one sorbent recycling subsystem and configured to monitor at least one parameter of said sorbent within said sorbent recycling subsystem. object control system. An emission control method for removing contaminants from an emission, comprising:
sending the effluent to a treatment system comprising an inverted venturi fluidized bed apparatus containing at least one adsorbent that chemically bonds with contaminants contained in the effluent;
directing the effluent away from the reverse venturi fluidized bed device;
selecting the at least one adsorbent from the group of materials comprising carbon-based adsorbents and further comprising copper, zinc, tin, sulfur (CZTS) having the molecular formula CuZnSnS, CZTS alloys, or combinations thereof;
sending said at least one sorbent through one or more chemical cleaning and regeneration sorbent recycling subsystems, said sorbent recycling subsystem containing chemical reagents for separating contaminants from said at least one sorbent; and wherein said chemical reagent is a fatty alcohol. 18. The method of controlling effluents of claim 17, further comprising: separating depleted and depleted sorbent from said sorbent sent through said sorbent recycling subsystem; and disposing of said depleted and depleted sorbent. death,
separating contaminants from the sorbents sent through the sorbent recycling subsystem and discarding or recycling the contaminants;
returning the recycled adsorbent to the reverse venturi fluidized bed apparatus;
A method of effluent control comprising the step of feeding fresh adsorbent to said reverse venturi fluidized bed apparatus to replace said exhausted and worn adsorbent. 19. The method of claim 18, wherein the at least one sorbent recycling subsystem comprises:
a first sorbent recycling subsystem dedicated to processing said CZTS;
a second sorbent recycling subsystem dedicated to processing the CZTS alloy;
and a third sorbent recycling subsystem dedicated to processing carbon-based sorbents. 20. The effluent control method of claim 19, further comprising: maintaining different adsorbents separate from each other within the inverted venturi fluidized bed apparatus;
detecting at least one process parameter of the reverse venturi fluidized bed apparatus by at least one monitoring sensor;
directing the effluent through one or more different adsorbents based on the at least one process parameter detected by the at least one monitoring sensor;
passing the CZTS through the first sorbent recycling subsystem;
passing the CZTS alloy through the second sorbent recycling subsystem;
A method of controlling emissions, comprising passing said carbon-based sorbent through said third sorbent recycling subsystem.

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