RU2547117C2 - Compact concentrator of effluents and gas-flushing unit for removal of contaminants - Google Patents

Abstract

FIELD: process engineering.

SUBSTANCE: proposed concentrator comprises gas inlet pipe, gas discharge outlet and flow channel communicating gas inlet pipe and gas discharge outlet. Note here that flow channel comprises contracted section to increase has flow rate therein. Fluid inlet pipe injects fluid in gas flow upstream of contracted section so that gas-fluid mix is completely mixed in flow section to cause the fluid partial evaporation. Mist separator or gas flushing unit downstream of contracted section removes trapped fluid drops from gas flow to return collected fluid into fluid inlet pipe via circulation circuit. Fresh fluid fed for concentration is forced into circulation circuit at the rate sufficient for compensation for fluid evaporated in said flow section.

EFFECT: concentrator can readily be connected to waste heat sources for concentration of fluid.

30 cl, 17 dwg

Description

Related Applications

This application is partly a continuation of the application for US patent No. 12/705,462, filed February 12, 2010, which is partly a continuation of the application of US patent No. 12/530,484, filed September 9, 2009, which is the national phase of the US international application PCT / US08 / 56702, filed March 12, 2008, stating the priority of provisional application for US patent No. 60/906,743, filed March 13, 2007. This application also claims the priority of provisional application for US patent No. 61/152,248, filed February 12, 2009 ., and provisional patent application US No. 61,229,650, filed 29 July 2009, each of the applications No. 12 / 530,484; 60 / 906,743; 61 / 152.248; and 61 / 229,650 is fully disclosed and incorporated herein by reference.

FIELD OF THE INVENTION

This application relates, in general, to liquid concentrators, in particular to compact, mobile, inexpensive wastewater concentrators that can easily be connected to waste heat sources and used to concentrate the liquid.

State of the art

Concentration of volatile substances can be an effective form of treatment or pre-treatment of a wide variety of wastewater, and it can be carried out as part of commercial treatment systems of various types. With a high level of concentration, many wastewater can be turned into waste that has the consistency of sludge, with a high content of dissolved and suspended substances. Such concentrated waste can be easily cured by the usual methods used in landfills, or, if appropriate, they are sent for further processing before final disposal. Concentration of wastewater can significantly reduce freight costs and the need for storage and can contribute to further recovery of materials from wastewater.

Industrial wastewater is very different from each other in its parameters, since they are formed during many industrial processes. Wastewater is generated not only in the normal operation of industrial enterprises, but also as a result of uncontrolled events that occur during breakdowns, accidents and natural disasters. With the resulting wastewater, proceed as follows: immediately sent to the treatment plant; subjected to pre-treatment, and then sent to treatment facilities; subjected to processing at the place of their formation or outside the place of their formation with the aim of disposing of valuable components or subjected to processing at the place of their formation or outside the place of their formation with the aim of simple preparation for final disposal. If the source of the wastewater is an uncontrolled event, an effective way to isolate and regenerate the strait should be included in any of the wastewater disposal scenarios.

An important parameter characterizing the effectiveness of the method for concentrating wastewater is the ratio of the volume of the residue after concentration to the volume of wastewater received for concentration. It is desirable to achieve low ratios of residual volume to the volume of incoming wastewater (high levels of concentration). If the wastewater contains dissolved and / or suspended non-volatile substances, the reduction in volume that can be achieved using a specific concentration method based on the evaporation of volatile substances is largely determined by the selected method of heat transfer of the treated liquid.

Conventional methods used for concentration by evaporation of water and other volatile substances can be divided into direct heat transfer systems and indirect heat transfer systems, depending on the method used to transfer heat to the liquid to be concentrated (process liquid). Indirect heat transfer devices include jacketed vessels filled with process fluid, or plate, submersible tubular or coil heat exchangers that are immersed in process fluid. In order to supply the heat necessary for evaporation, a heating medium such as water vapor or hot oil is passed through shirts or heat exchangers. Direct heat transfer devices in which the heating medium is brought into direct contact with the process fluid are used, for example, in systems with an immersion combustion chamber.

The effectiveness of indirect heat transfer systems that use heat exchangers, such as shirts, plate, immersion pipes or coils, is usually limited by the formation of solid deposits on the surfaces of heat exchangers in contact with the process fluid. The design of such systems is also complicated by the need to have a separate device for transferring heat to the coolant, such as a steam boiler, or a device used to heat another coolant, such as an oil heater. This design is limited to the use of two indirect heat transfer systems for concentration. Those liquids that form precipitates on heat exchangers during heating are called scale-forming liquids. If liquids contain certain compounds, such as carbonates, in which solubility decreases with increasing temperature, a precipitate, usually called scale, will form even at a relatively low concentration due to the high temperature on the surface of the heat exchanger. In addition, if compounds having high solubility at high temperatures, such as sodium chloride, are present in the wastewater, they will also precipitate after reaching a high concentration. Precipitates, which often have to be removed from the surface of the heat exchanger to ensure heating efficiency, can be a mixture of suspended solids brought in by wastewater and solids precipitated from the process fluid. The negative effect of the deposition of solids on the surface of the heat exchanger is to reduce the time during which indirect heat transfer can take place before you have to stop working for another cleaning. This negative impact introduces a limit on the amount of wastewater that can be effectively heated, especially if scale-forming liquids are included in the wastewater. Therefore, methods operating on the principle of indirect heat transfer are generally unsuitable for concentrating most of the wastewater and providing a low ratio of the volume of the residue to the volume of incoming wastewater.

U.S. Patent No. 5,342,482, which is incorporated herein by reference, describes a specific type of direct heat transfer concentrator that implements a bubble heat transfer method in which gaseous combustion products are generated and fed through an inlet pipe to a dispersing device immersed in a process liquid. The dispersing device comprises several exhaust pipes located at a distance from each other, diverging radially from the intake pipe, each exhaust pipe having small openings located at a distance from each other at different places on the surface of the exhaust pipe so that gaseous combustion products can be released in the form of small bubbles as uniformly as practicable over the entire cross section of the liquid subjected to heating in a working state de. According to modern concepts of known devices of this type, this concentrator provides the required close contact between the liquid and the hot gas on a large interface. The peculiarity of this method is that both heat transfer and mass transfer occur under dynamic conditions on a constantly updated interfacial surface resulting from the bubbling of the gas phase through the process fluid, and not on the solid surface of the heat exchanger, on which solid particles can settle. Thus, the bubbling process implemented in this concentrator provides significant advantages over conventional indirect heat transfer processes. However, the small openings in the exhaust pipes that are used to distribute the hot gases over the volume of the process fluid in the concentrator according to US Pat. No. 5,342,482 are clogged with solids deposited from scale-forming liquids. As a result, the inlet pipe, through which hot gases are supplied to the process fluid, is covered with a crust of solid sediment.

Because of the need to pass a large volume of gas through a continuously flowing liquid phase stream, the vessel with the concentrator proposed in US Pat. No. 5,342,482 typically has to have a large cross section. The inner surface of such a vessel and any fittings installed inside it is called the “wetted surface” of this method. This wetted surface must withstand the effects of varying concentrations of the hot process fluid during system operation. In systems designed for the treatment of a wide variety of wastewater, structural materials of a wetted surface require special design solutions with regard to corrosion resistance and temperature resistance, which should take into account the cost of equipment and the cost of its maintenance and replacement after a certain time. Generally speaking, increasing the service life and lowering the cost of maintenance / replacement of the wetted surface is ensured by choosing either high-quality metal alloys or certain structural plastics, such as those used for the production of fiberglass vessels. However, conventional concentration methods using indirect or direct heating systems also require devices for supplying hot fluids, such as water vapor, oil or gas, capable of heating the liquid in the vessel. Although many high-quality alloys meet the requirements for corrosion resistance and temperature resistance, the vessels and fittings made from them are too expensive. On the other hand, although structural plastics can be used to make the entire vessel as a whole or as a coating on a wetted surface, the low temperature resistance does not allow the use of many structural plastics. For example, the high temperature of the inlet pipe, designed to supply hot gas inside the vessel according to US patent No. 5442482, does not allow the use of structural plastics for its manufacture. Thus, the production of vessels and other equipment used to implement these methods, and their maintenance are very expensive.

In addition, a heat source is required in all of these systems so that concentration or evaporation can be carried out. Many systems have been developed that use heat generated by various sources, for example, heat generated by an engine, combustion chamber or gas compressor, as a heat source for treating wastewater. One such system is described in US Pat. No. 7,214,290. In this system, heat is generated during the combustion of gas generated from organic waste and is used in a submersible gas evaporator to treat waste water in a landfill. US Pat. No. 7,416,172 describes a submersible gas vaporizer in which waste heat can be supplied to the gas vaporizer inlet so that it can be used to concentrate or evaporate liquids. Although waste heat is considered a cheap source of energy, for its effective use in wastewater treatment, waste heat in many cases has to be transported a considerable distance from the source of waste heat to the place where evaporation or concentration is carried out. For example, in many cases, electric generators will operate in a landfill that use one or more internal combustion engines that use gas released from organic waste as fuel. The exhaust gases of these engines, which are usually emitted through a silencer and exhaust pipe into the atmosphere on the roof of the building where the electric generators are located, are a source of waste heat. But in order to collect and use this waste heat, you need to connect a significant amount of expensive pipes and pipelines to the exhaust pipe and supply waste heat through them to the place where the processing system is located, which is usually placed at zero mark far from the building where the generators are located. It should be noted that pipes, pipelines and regulating devices (for example, throttle or shut-off valves) are made of expensive materials that can withstand high temperatures that have exhaust gases in the exhaust pipe (for example, 510 ° C), and must be insulated so that the exhaust gases did not cool during transportation. The materials used to isolate them are prone to destruction under the influence of many factors, such as brittleness, a tendency to erosion after a certain time, and sensitivity to cyclic temperature fluctuations, which further complicates the design. Insulation also increases the mass of pipes, pipelines and control devices, which leads to an increase in the cost of supporting structures.

Disclosure of invention

The compact device for concentrating liquids proposed here can easily be connected to a source of waste heat, such as a torch for burning gas emitted from organic waste, or an exhaust pipe of an internal combustion engine, and use this waste heat to conduct a direct heat transfer concentration method without using large, expensive vessels and many expensive temperature-resistant materials. The compact fluid concentrator comprises a gas inlet, a gas outlet and a mixing or flow channel connecting the gas inlet to the gas outlet, the flow channel having a narrowed portion in which the gas flow rate through the flow channel increases. Through the liquid supply pipe located between the gas inlet and the narrowed section of the flow channel, liquid is injected into the gas stream at a point in front of the narrowed section so that the gas-liquid mixture is completely mixed in the flow channel, resulting in evaporation or concentration of a portion of the liquid. In the mist eliminator or scrubber located behind the narrowed section and connected to the gas outlet, liquid droplets carried away by the gas stream are separated, and the collected liquid is returned to the nozzle for supplying it along the recirculation circuit. Fresh liquid entering the concentration is also introduced into the recirculation loop at a speed sufficient to compensate for the total decrease in the amount of liquid due to its evaporation in the flow channel and due to the discharge of concentrated liquid.

The proposed compact fluid concentrator has a number of features that provide cost-effective concentration of wastewater, very different from each other in their parameters. The concentrator has corrosion resistance in relation to wastewaters, which differ greatly in their parameters, have a moderate manufacturing cost and reasonable operating costs, are able to operate continuously with a high degree of concentration, and efficiently use thermal energy directly from many sources. In addition, the concentrator is compact enough to be transported to places where waste water was generated as a result of uncontrolled events and installed directly near waste heat sources. Thus, the proposed concentrator is a cost-effective, reliable device with a long service life, which continuously concentrates wastewaters that are very different from each other in their parameters, and thus can dispense with conventional heat exchangers with a solid heat exchange surface used in conventional systems with indirect heat transfer, which are clogged and overgrown with a crust of scale.

Brief Description of the Drawings

Figure 1 shows the General scheme of a compact fluid concentrator.

FIG. 2 shows an embodiment of a fluid concentrator, the circuit of which is shown in FIG. 1 mounted on a liquid sump or slide to facilitate transportation by truck.

Figure 3 shows a perspective image of a compact liquid concentrator, which implements the concentration method, the scheme of which is shown in figure 1, connected to a source of waste heat, which is a torch for burning gas released from organic waste.

Figure 4 shows the image and perspective of the heat transfer unit of the compact fluid concentrator shown in figure 3.

Figure 5 shows a perspective view of the evaporation / concentration unit of the compact liquid concentrator shown in figure 3.

Figure 6 shows a perspective view of easily opening inspection hatches on the unit of the compact fluid concentrator shown in figure 3.

In Fig.7 shows a perspective image of the open state of one of the easily opened inspection hatches depicted in Fig.6.

On Fig shows a perspective image of an easily openable locking mechanism used on the inspection hatches depicted in Fig.6 and 7.

Fig. 9 is a schematic illustration of a control system that can be used to adjust various units in the compact fluid concentrator shown in Fig. 3.

Figure 10 shows the image of the compact fluid concentrator shown in figure 3, which is connected to the exhaust pipe of the combustion engine as a source of waste heat.

11 is a schematic illustration of another embodiment of a compact fluid concentrator.

On Fig shows a top view of the compact fluid concentrator shown in Fig.11.

13 is a schematic illustration of a third embodiment of a compact fluid concentrator, which is a distributed fluid concentrator.

FIG. 14 is an enlarged cross-sectional view of the fluid concentration unit of the distributed fluid concentrator shown in FIG. 13.

On Fig shows a top view of the block of concentration of the liquid shown in Fig.

FIG. 16 is a side view of the closed cooler unit and the venturi section of the distributed fluid concentrator shown in FIG. 13.

FIG. 17 is a perspective view of an alternative embodiment of a compact fluid concentrator providing the concentration method of FIG. 1 and configured to remove ammonia from landfill filtrates.

The implementation of the invention

Figure 1 shows a General diagram of a fluid concentrator 10, which contains a gas inlet 20, a gas outlet 22 and a flow channel 24 connecting the gas inlet 20 to the gas outlet 22. The flow channel 24 has a narrowed portion 26, which increases the speed of gas flow through the flow channel 24 and in this place or near it in the flow channel 24 there is a turbulent flow. The narrowed portion 26 in this embodiment may be a venturi device. Through the fluid supply pipe 30, the liquid to be concentrated (by evaporation) is injected into the fluid concentration chamber in the flow channel 24 at a point in front of the narrowed portion 26, and the injected fluid is mixed with the gas stream in the flow channel 24. The fluid supply pipe 30 may comprise one or more interchangeable nozzles 31, designed to inject liquid into the flow channel 24. The inlet pipe 30, regardless of whether it contains a nozzle 31 or not, can supply liquid to the flow channel 24 under any angle, including perpendicular and parallel to the gas flow. Near the nozzle for supplying fluid 30 may also be a partition 33 in such a position that the fluid coming from the nozzle 30 is reflected from it into the flow channel in the form of small drops.

When a gas-liquid stream flows through a narrowed portion 26 according to the Venturi effect, the speed increases and a turbulent flow arises, which completely mixes the gas and liquid in the flow channel 24 near the pipe 30 and behind it. The acceleration when flowing through the narrowed portion 26 creates transverse forces acting between the gas flow and the liquid droplets, as well as between the liquid droplets and the walls of the narrowed portion 26, which leads to the formation of very small liquid droplets involved in the gas, thus increasing the boundary area surfaces between liquid droplets and gas, and facilitating the rapid transfer of mass and heat between gas and liquid droplets. The fluid exits the narrowed portion 26 in the form of very small drops of liquid, regardless of the geometric shape of the fluid entering the narrowed portion 26 (for example, the fluid may enter the narrowed portion 26 in the form of a film). As a result of turbulent mixing and the action of transverse forces, part of the liquid quickly evaporates and becomes a component of the gas stream. When the gas-liquid mixture flows through the narrowed portion 26, the direction and / or flow rate of the gas-liquid mixture can be changed using adjustable flow restrictors, such as a venturi 32, which is generally used to create a large pressure drop in the flow channel 24 before and after the venturi 32. The position of the Venturi plate 32 can be adjusted to change the size and / or shape of the narrowed portion 26, and it can be made of corrosion-resistant material, including high-quality alloys, such ak "Hastelloy", "Inconel" or "Monel".

From the narrowed portion 26, the gas-liquid mixture enters a mist eliminator 34 (also called a gas scrubber or drop eliminator) connected to the gas outlet 22. The mist eliminator 34 removes droplets of liquid that it has carried away from the gas stream. The mist eliminator 34 comprises a gas passage. The separated liquid accumulates in the liquid collector or liquid sump 36 in this gas passage, the liquid sump 36 may be provided with a vessel for storing the collected liquid. A pump 40 may be connected to the liquid sump 36 and / or to this vessel, for supplying the liquid through the recirculation circuit 42 back to the liquid supply pipe 30 and / or the flow channel 24. Thus, the liquid volume can be reduced by evaporation to the required degree concentration. Fresh or new liquid, aimed at concentration, is fed into the recirculation circuit 42 through the liquid supply pipe 44. Instead, this new liquid can be injected directly into the flow channel 24 in front of the venturi 32. The rate of supply of fresh liquid to the recirculation circuit 42 may equal the sum of the evaporation rate liquid during the passage of the gas-liquid mixture through the flow channel 24 and the rate of liquid withdrawal through the nozzle for the selection of concentrated liquid 46 located on the vessel or near the vessel for storage ia separated liquid 40. The ratio of the volume of circulating liquid to the volume of fresh liquid can generally be in the range of 1: 1 to 100: 1, but is usually in the range of 5: 1 to 25: 1. For example, if in the recirculation loop 42 the fluid circulates at a speed of about 10 gallons / min, then fresh or new fluid can be supplied at a speed of about 1 gallon / min (i.e., in a ratio of 10: 1). Part of the fluid can be drawn through the nozzle for collecting concentrated liquid 46 after the liquid in the recirculation circuit 42 reaches the desired concentration level. The recirculation circuit 42 acts as a buffer or shock absorber in the evaporation method, ensuring that there is sufficient moisture in the flow channel 24 to prevent complete evaporation of the liquid and / or to prevent the formation of dry particles.

After passing through the mist eliminator 34, the gas stream enters the exhaust fan 50, which sucks the gas through the flow channel 24 and the gas passage of the mist eliminator, creating a vacuum. Of course, the concentrator 10 could also work at elevated pressure created by a gas blower (not shown in the figure) placed in front of the fluid supply pipe 30. Finally, the gas is released into the atmosphere through the gas outlet 22 or is sent for further processing.

The concentrator 10 may comprise a pre-treatment system 52 for treating a concentrated liquid, which may be wastewater. For example, an air deodorizer can be used as a pretreatment system 52 to remove substances that can create a nasty smell or are controlled as air pollutants. In this case, the air deodorizer may be a conventional type air deodorizer, or it may be another concentrator of the type proposed here that can be connected in series as an air deodorizer. In the pretreatment system 52, the concentrated liquid may, if necessary, be heated by any suitable method. In addition, the gas and / or wastewater circulating through the concentrator 10 can be preheated in the heater 54. Preheating can be used to increase the rate of evaporation, and therefore the rate of concentration of the liquid. Preheating of gas and / or wastewater can be done by burning renewable fuels, such as wood chips, biogas, methane or mixtures thereof, fossil fuels, or by using waste heat. In addition, preheating of the gas and / or wastewater can be done by using the waste heat generated in a chimney or flare to burn gas generated from organic waste. Waste heat from an engine, such as an internal combustion engine, can also be used to preheat the gas and / or wastewater. Also, natural gas can be used as a source of waste heat, natural gas can be supplied directly from the mouth of the gas well in an uncleaned state or immediately after the completion of the gas well’s equipment until the gas flow is stabilized or after the gas flow is stabilized in the more established mode of the natural gas well. Additionally, natural gas can be purified before being flared. In addition, the gas stream exiting the gas outlet 22 of the concentrator 10 can be fed to a flare unit or some other device for subsequent processing 56, designed to process the gas before it is discharged into the atmosphere.

The fluid concentrator 10 provided herein can be used to concentrate a variety of wastewater, such as industrial wastewater, wastewater generated during natural disasters (floods, hurricanes), depleted caustic, or filtrates, such as landfill filtrates, return water from completed natural gas wells, formation water obtained during the operation of natural gas wells, etc. The fluid concentrator 10 is convenient to operate, energy-efficient, reliable and cost-effective. The usefulness of this fluid concentrator is further enhanced by the ability to install the fluid concentrator 10 on a trailer or mobile skid so that it can successfully handle wastewater generated during accidents and natural disasters, or used for regular treatment of wastewater generated in spatially isolated or remote objects. The liquid concentrator 10 proposed here has all the required parameters and provides significant advantages over conventional liquid concentrators, especially when it is necessary to treat a wide variety of wastewater.

In addition, the concentrator 10 can be made predominantly of low cost materials having high corrosion resistance, such as fiberglass and / or other structural plastics. This possibility is partly due to the fact that the proposed hub is designed to operate at a minimum differential pressure. For example, differential pressure should generally have a value in the range of 10 to 30 inches of water column. And since in the zone of gas-liquid contact, when the concentration method is introduced, strong turbulence occurs inside the limited (compact) passage in the area with the Venturi profile or directly behind it, the whole structure is very compact in comparison with conventional concentrators in which gas contact with liquid flows in a large technological vessel. As a result, the amount of high-quality metal alloys required for the manufacture of the hub 10 is rather small. And since the size of parts made of high-quality alloys is small and these parts can easily be replaced in a short period of time with minimal labor, manufacturing costs can be cut even more by designing some of these wearing parts or all of these wearing parts from lower-quality alloys and by periodically replacing them. If necessary, corrosion-resistant and / or erosion-resistant lining material, such as structural plastics, including elastomeric polymers, can be applied to these lower-quality alloys (for example, carbon steel) to increase the service life of such parts. Similarly, pump 40 can be coated with a corrosion resistant and / or erosion resistant lining material to increase the life of the pump 40 and thereby further reduce maintenance and replacement costs.

It is understood that the liquid concentrator 10 provides direct contact of the liquid to be concentrated with the hot gas, creating heat transfer and mass transfer between the hot gas and the liquid, for example, concentrated waste water, in a highly turbulent mode. In addition, the concentrator 10 creates a very compact zone of gas-liquid contact, making it minimal in size in comparison with known concentrators. The heat exchange produced by direct contact increases energy efficiency and makes heat exchangers with a solid heat exchange surface unnecessary, which are used in conventional concentrators with indirect heat transfer, unnecessary. In addition, the compact gas-liquid contact zone makes bulky process vessels used in conventional indirect or direct heat transfer concentrators unnecessary. These features make it possible to manufacture a concentrator 10 of small mass in comparison with conventional concentrators using relatively cheap manufacturing techniques. Both of these factors increase its portability and profitability. Thus, the fluid concentrator 10 is more compact and lightweight than conventional concentrators, which makes it ideally suited as a mobile unit. In addition, the fluid concentrator 10 is less prone to clogging and clogging due to heat transfer by direct contact and the absence of solid heat transfer surfaces. Due to heat exchange by direct contact, the liquid concentrator 10 can also be used to process liquids containing a significant amount of suspended substances. As a result, a high degree of concentration can be achieved without frequent cleaning of the concentrator 10.

In particular, in liquid concentrators that use indirect heat transfer, heat exchangers are prone to clogging and are subject to accelerated corrosion at normal operating temperatures of the coolant circulating in them (steam or other hot fluid). Each of these factors imposes significant limitations on the service life and / or cost of constructing conventional concentrators with indirect heat transfer, as well as how long they can work before stopping them and cleaning or repairing the heat exchangers. As a result of the rejection of bulky technological vessels, the mass of the liquid concentrator, as well as the initial cost and the cost of replacing parts made of high-quality alloys, are significantly reduced. In addition, due to the temperature difference between the gas and the liquid, the relatively small volume of the liquid in the system, and the low relative humidity of the gas before mixing it with the liquid, the concentrator 10 operates at a temperature close to the adiabatic saturation temperature of a particular gas-liquid mixture, which usually has a value of range from 150 ° F to 215 ° F (ie, the concentrator is a "low inertia" concentrator).

In addition, the concentrator 10 is designed to work under vacuum, which greatly contributes to the use of a wide variety of fuels or sources of waste heat as an energy source for evaporation. In fact, due to the flow-through design of these systems, supercharged and naturally aspirated burners can be used to heat and supply gas to the concentrator 10. The simplicity of design and the reliability of the hub 10 are ensured by a minimum number of moving parts and a minimum need for spare parts. In general, a concentrator needs only two pumps and one exhaust fan if it is designed to work with waste heat, such as exhaust gases from engines (such as a generator engine or a car), flue gases from industrial pipes, gas compressor systems, and flare plants used for example, for burning gas released from organic waste. These features provide significant advantages in that they have a beneficial effect on operational flexibility and the costs of purchasing, operating and maintaining a hub 10.

The hub 10 may operate in a start state or steady state. In the start-up state, the mist eliminator 34 and the recirculation circuit 42 can be filled with fresh wastewater. During the initial treatment, fresh wastewater entering the fluid supply pipe 30 is at least partially vaporized in the narrowed portion 24 and settles in the settling tank of the mist eliminator 34 in a more concentrated form than fresh wastewater. After a certain time, the wastewater reaches in the sump of the mist eliminator 34 and the recirculation circuit 42 of the desired concentration level. From this moment, the concentrator 10 can operate in a continuous mode, in which the amount of solid particles discharged into the pipe for collecting concentrated liquid 46 is equal to the number of solid particles entering fresh wastewater through the pipe for supplying liquid 30. In the same way, the amount of water evaporated in the concentrator 10, is replaced by an equal amount of water in fresh wastewater. Thus, the concentrator 10 operates at a temperature close to the adiabatic saturation temperature of the mixture of heated gas and liquid. The result is a high efficiency of the hub 10.

FIG. 2 is a side view of a fluid concentrator 10 mounted on a movable bed 60, such as a fluid sump, trailer, or slide. The mobile bed is sized and shaped so that it can be easily loaded onto a vehicle or attached to a vehicle 62, such as a tractor with a trailer. Similarly, a hub mounted on such a bed can easily be loaded onto a train, ship or plane (not shown in the figure) to quickly deliver to remote locations. The fluid concentrator 10 can operate as a fully autonomous installation having its own burner and fuel supply system, or the fluid concentrator 10 can use a burner and / or a source of fuel or waste heat available at the place of use. The fuel for the hub 10 may be renewable fuels such as waste (e.g. paper or wood chips) and gas generated from organic waste. In addition, the concentrator 10 can operate on any mixture of traditional fossil fuels, such as coal or oil, renewable fuels and / or waste heat.

A typical hub 10 mounted on a trailer is capable of processing at least one hundred thousand gallons of wastewater per day, while larger stationary units that are installed in landfills, wastewater treatment plants or gas or oil fields are capable of processing hundreds of thousands of gallons of wastewater per day.

FIG. 3 shows a specific embodiment of a compact fluid concentrator 110 that operates using the principles described above with reference to FIG. 1, which is connected to a waste heat source in the form of a flare unit for burning gas generated from organic waste. Generally speaking, the compact fluid concentrator 110 shown in FIG. 3 is designed to concentrate wastewater, such as landfill filtrate, using the waste or waste heat generated in the flare unit during the combustion of gas generated from organic waste, thus, as indicated in the standards of the United States Environmental Protection Agency (EPA) and / or more local regulatory authorities. As you know, most landfills have a flare unit used to burn gas released from organic waste to remove methane and other gases from it before they enter the atmosphere. Typically, the gas leaving the flare unit has a temperature in the range of 1200 ° F to 1500 ° F, but can also heat up to 1800 ° F. The compact fluid concentrator 100 shown in FIG. 3 is equally effective in concentrating return water or produced water from natural gas wells and can use flue gas from a natural gas flare unit, or a propane flare unit located at or near the wellhead. In some applications, the supply of natural gas to a flare unit of natural gas can be carried out directly from a natural gas well.

As shown in FIG. 3, a compact fluid concentrator 110 is typically connected to a flare unit 115 and comprises a heat transfer unit 117 (shown in an enlarged view of FIG. 4), an air pre-treatment unit 119, a concentration unit 120 (shown in an enlarged view of FIG. .5), a gas washing unit 122 and an exhaust unit 124. An important feature is that the flare unit 115 comprises a torch 130 in which, in some known manner, gas generated from organic waste is burned and a flare-cap unit 132. Flare-flask The check block 132 comprises a hinged cap 134 (for example, a flare cap or an exhaust cap) that closes on top a torch 130 or a different type exhaust pipe (for example, a flue gas exhaust pipe) when the flare cap 134 is in the closed position or removes part of the flare gas when the flare gas is partially covered, and which allows the flue gas generated in the flare 130 to escape into the atmosphere through the open end, which forms the primary gas outlet 143, when the flare cap 134 is open or partially open position. The flare cap 132 also includes a cap drive 135, such as an motor (for example, an electric motor, a hydraulic motor or a pneumatic motor shown in FIG. 4), which moves the flare cap 134 between a fully open position and a fully closed position. As shown in FIG. 4, the flare cap drive 135 may, for example, rotate the flare cap 134 around the hinge axis 136, opening and closing the flare cap 134. The flare cap drive 135 may use a chain drive or some other type of drive mechanism connected to the flare cap 134 to rotate the flare cap 134 around the hinge axis 136. The flare cap block 132 may also comprise a counterweight 137 located on the opposite side of the hinge axis 136 of the flare cap 134 so that balance the weight of the flare cap 134 while the flare cap 134 is moved around the pivot axis 136. The counterweight 137 allows the drive 135 to be reduced in size or power so that it can still turn the flare cap 134 between the open position in which the top of the torch 130 ( or the primary gas outlet 143) is open to the atmosphere, and in a closed position in which the flare cap 134 substantially seals the upper end of the torch 130 (or primary gas outlet 143). The flare cap 134 itself can be made of a material with high temperature resistance, such as stainless steel or carbon steel, and can be lined with refractory material, for example, aluminum oxide and / or zirconium oxide, from the lower side, which is in direct contact with hot flare gases, when the flare cap 134 is in the closed position.

If necessary, the torch 130 may be provided with a transition device 138 comprising a primary gas outlet 143 and a secondary gas outlet 141 in front of the primary gas outlet 143. When the torch cap 130 is in the closed position, flue gases are discharged through the secondary gas outlet 141. The transition device 138 may have a fitting 139 that connects the torch 130 (or chimney) to the heat transfer unit 117 via a 90 degree bend or bend. Other connectors may also be used. For example, the torch 130 and the heat transfer unit 117 can be connected, in essence, at any angle in the range from 0 to 180 degrees. In this case, the flare-cap block 132 is mounted on top of the adapter 138 near the primary gas outlet 143.

As shown in FIGS. 3 and 4, the heat transfer unit 117 comprises a heat transfer pipe 140 that connects the inlet pipe of the air pre-treatment unit 119 to the torch 130, and more specifically, to the adapter 138 of the torch 130. The heat transfer pipe 140 between the torch 130 and the pre-heat unit air treatment 119 lies at a certain height above the ground, resting on a rack in the form of a vertical beam or column. The heat transfer pipe 140 is connected to a fitting 139 or to a secondary gas outlet 141 of the adapter 138, forming a duct between the adapter 138 and a device for conducting a secondary process, such as concentration of a liquid. A support post 142 is usually not enough, since the heat transfer pipe 140 is made of metal, such as carbon or stainless steel, and can be lined with materials such as aluminum oxide and / or zirconia so that it can withstand the temperature of the gas coming from the flare 130 to the air pre-treatment unit 119. Thus, the heat transfer pipe 140 is usually a heavy part of the equipment. However, the torch 130, on the one hand, and the air pre-treatment unit 119, and the concentrating unit 120, on the other hand, are located directly next to each other, so the heat transfer pipe 140 should be relatively short, which helps to reduce the cost of materials used in the concentrator 110, as well as the cost of the supporting structures holding the heavy parts of the concentrator 110 above the ground. As shown in FIG. 3, the heat transfer pipe 140 and the air pretreatment unit 119 form a U-shaped structure with its legs facing down.

The air pre-treatment unit 119 comprises a vertical pipe 150 and an atmospheric air inlet valve (not shown explicitly in FIGS. 3 and 4) located on top of the pipe 150. The atmospheric air inlet valve (also called an air valve) forms a duct between the heat transfer pipe 140 ( or air pre-treatment unit 119) and the atmosphere. The atmospheric air inlet valve allows atmospheric air to enter through the wire shield 152 used for protection from birds and mix inside the unit for pre-treating air 119 with hot gas coming from the torch 130. If necessary, the unit for pre-treating air 119 may have a constantly open a window near the air valve, which can always let a certain amount of air into the air pre-treatment unit 119, and this window allows you to reduce the size of the uemogo air valve and increase the operational safety of the hub. A pressure supercharger (not shown) can be connected, if necessary, to the inlet side of the atmospheric air valve to enhance the passage of atmospheric air through the atmospheric air valve. When using a pressure supercharger, a bird shield 152 and a constantly open window (if used) can be connected to the inlet side of the pressure supercharger. Although controlling the operation of the atmospheric air inlet valve or air valve will be discussed in more detail below, it should be noted that this valve allows the gas coming from the torch 130 to be cooled to a more acceptable temperature before it enters the concentrating unit 120. The pre-treatment unit of air 119 may partially rely on the cross members 154 attached to the support post 142. The cross members 154 stabilize the air pre-treatment unit 119, which is usually also made of heavy carbon distilled or stainless steel or from another metal and which can be lined to increase energy efficiency and temperature resistance in this section of the concentrator 110. If necessary, the vertical pipe 150 can be extended so that it can be used for torches of different heights, and thereby make a fluid concentrator 110 suitable for a variety of different flares or for flares of different heights. This principle is explained in more detail with reference to figure 3. As shown in FIG. 3, the vertical pipe 150 comprises a first section 150A (shown by dashed lines) that enters the second section 150B and thereby allows the length (height) of the vertical pipe 150 to be adjusted.

Generally speaking, the air pretreatment unit 119 serves to mix the atmospheric air entering through the atmospheric air inlet valve under the wire shield 152 with the hot gas coming from the torch 130 through the heat transfer pipe 140 to obtain a gas having a desired inlet temperature into the concentrating unit 120.

The concentrating unit 120 comprises a guiding portion 156 with a decreasing cross section, the upper end of which is mated to the lower end of the vertical pipe 150, and the lower end to the cooler 159 of the concentrating unit 120. The concentrating unit 120 also contains a first fluid inlet 160 through which a new or untreated liquid sent for concentration, such as landfill filtrate, is injected into the cooler 159. The nozzle 160 may contain, although not shown in FIG. 3, a large droplet atomizer with a nozzle a large cross-section for injecting untreated fluid into the cooler 159. The fluid injected into the cooler 159 at this point in the system has not yet been concentrated, and therefore contains a large amount of water, and the spray has a large cross-section, so the nozzle of the spray is not contaminated or clogged with small particles contained in the liquid. It is understood that the cooler 159 is designed to rapidly lower the temperature of the gas stream (for example, from 900 ° F to 200 ° F) as a result of strong evaporation of the liquid injected through the inlet pipe 160. If necessary, it can be installed, although not shown in FIG. 3, the temperature sensor at the outlet or near the outlet of the pipe 150 or in the cooler 159 and use it to regulate the position of the shut-off element of the intake valve of the atmospheric air and thereby to control the temperature of the gas in the inlet pipe of the concentrating unit and 120.

As shown in FIGS. 3 and 5, the cooler 159 is connected to a liquid injection chamber connected to a narrowed section or a section with a venturi profile 162, which has a narrowed cross section compared to the cooler 159 and which contains a venturi plate 163 (shown in dashed lines). The venturi plate 163 creates a narrowed passage in the section with the venturi profile 162, which leads to a large pressure drop between the inlet and outlet of the section with the venturi profile 162. This large pressure drop creates a turbulent gas flow in the cooler 159 and in the upper part or at the entrance of the section with venturi profile 162 and causes gas to flow out of the area with venturi profile 162 at a high speed, and all this leads to complete mixing of gas and liquid in the area with venturi profile 162. The position of the venturi plate 163 can be adjusted with the knob oh manual control 165 (shown in figure 5) connected to the hinge axis of the plate 163, or using an electric motor or pneumatic cylinder (not shown in figure 5).

The recirculation pipe 166 encompasses the entrance to the section with the venturi profile 162 from opposite sides and serves to inject partially concentrated (i.e., circulated) liquid onto the section with the venturi profile 162 in order to further concentrate it and / or to prevent the formation of dry particles inside the concentration block 120 through a plurality of fluid inlets located on one or more sides of the flow channel. Although in Figures 3 and 5 explicitly not indicated on each of the opposite branches of the pipe 166, partially covering the portion with the profile of the venturi 162 may extend several tubes, e.g., three tubes of diameter _^1/2 inch, and penetrate inside wall portion with Venturi profile 162. Since the fluid entering the concentrator 110 at this point is a circulating fluid, it is therefore either partially concentrated or has reached a certain equilibrium concentration and is more likely to clog the spray nozzles than If concentrated liquid is injected through nozzle 160, then this liquid should be injected directly from the tubes, without nebulizers, to avoid clogging. However, if necessary, a baffle in the form of a flat plate can be installed in front of each half-inch tube opening to cause the liquid entering the system at this point to break into small droplets when it hits the baffle and disperse in the concentrating unit 120. Having this configuration, this recirculation system better distributes or sprays the recirculation fluid through the gas stream inside the concentrating unit 120.

The mixture of hot gas and liquid flows in a turbulent mode through a section with a venturi profile 162. As mentioned above, a section with a venturi profile 162, which has a movable venturi plate 163 located across the concentrating block 120, causes turbulence in the flow and complete mixing of the liquid and gas, contributing to the rapid evaporation of liquid in the gas. Since the mixing action exerted by the venturi 162 section provides a high degree of evaporation, the gas is substantially cooled in the concentrating block 120 and leaves the section with the venturi 162 profile at the flooded elbow 164 at high speed. In fact, the temperature of the gas-liquid mixture at this point can be about 160 ° F.

As usual for flooded elbows, a spillway device (not shown) at the bottom of the flooded elbow 164 maintains a constant level of partially or fully concentrated recirculated fluid entering it. Drops of recirculation liquid involved in the gas phase when the gas-liquid mixture leaves the area with the Venturi profile 162 are discharged at a high speed onto the surface of the recirculation liquid held in the lower part of the flooded knee 164 by centrifugal force that occurs when the gas-liquid mixture is forced to rotate 90 degrees to get into to the gas washing unit 122. A significant number of drops of liquid are involved in the gas phase, which collides with the surface of the recirculation liquid held in the lower part and the flooded elbow 164, is connected to the recirculation fluid, which leads to an increase in the volume of the recirculation fluid in the lower part of the flooded elbow 164 and to ensure that the amount of recirculation fluid flowing from the spillway device and flowing under the action of gravity into the sump 172 in the lower part of the gas washing unit 122. Thus, as a result of the interaction of the gas-liquid stream with the liquid in the flooded elbow 164, liquid droplets are removed from the gas-liquid stream and collisions are prevented e suspended particles contained in the gas-liquid stream with the bottom of the flooded elbow 164 at high speed, and thereby erosion of the metal wall of the flooded elbow 164 is prevented.

From the flooded elbow 164, a gas-liquid stream, which contains an evaporated liquid, a number of drops of liquid and other particles, enters the gas washing unit 122, which in this case is a cross-flow gas washing device. The gas-washing unit 122 contains different screens or filters that help remove entrained liquid from the gas-liquid stream and remove other particles that might be present in the gas-liquid stream. In one particular embodiment, the cross-flow gas-washing apparatus 122 may comprise a front coarse reflective baffle 169 at the inlet that is designed to remove liquid droplets ranging in size from 50 μm to 100 μm. Behind it, two interchangeable pleated filters 170 are located across the stream flowing through the gas washing unit 122, the filters 170 being able to gradually change size or configuration so that droplets of ever smaller size, such as 20-30 μm and less than 10 μm, can be removed. Of course, more or fewer filters or pleated filters can be used.

As in conventional cross-flow gas scrubbers, the liquid trapped in filters 169 and 170 and the overflow chamber in the lower part of the flooded bend 164 flows by gravity to a reservoir or liquid sump 172 located in the lower part of the gas washing block 122. A liquid sump 172, which can hold, for example, 200 gallons of liquid, thereby collecting concentrated liquid containing dissolved and suspended solids removed from the gas-liquid stream, and serves as a recirculation source concentrated concentrated liquid fed back to the concentrating unit 120 for further processing and / or to prevent the formation of dry particles in the concentrating unit 120 in the manner as described above with reference to FIG. In one embodiment, the liquid sump 172 may have an inclined V-shaped bottom 171 having a V-shaped trough extending from the rear side of the gas washing unit 122 (farthest from the flooded elbow 164) to the front side of the gas washing unit 122 (closest to the flooded elbow 164), wherein the V-shaped trough 175 is tilted so that the bottom of the V-shaped trough 175 is lower at the end of the gas washing unit 122 closest to the flooded elbow 164 than at the end of the gas washing unit 122 remote from the flooded elbow 164. In other words, V -shaped its bottom 171 can be tilted towards the lowest point of this V-shaped bottom 171, located near the cesspool 173 and / or pump 182. In addition, concentrated liquid from the liquid sump 172 can be pumped by a washing circuit pump (not shown in the figures) to a sprayer (not shown) inside the gas-washing unit 122, this sprayer for spraying liquid onto a V-shaped bottom. In addition, the concentrated liquid from the liquid sump 172 may be pumped by a wash circuit pump 177 (FIG. 9) to the atomizer 179 inside the cross-flow gas-washing unit 122, and this atomizer 179 is designed to spray liquid onto the V-shaped bottom 171. But the atomizer 179 can spray on the V-shaped bottom 171 and non-concentrated liquid or pure water. The atomizer 179 can periodically or continuously spray liquid onto the surface of the V-shaped bottom 171 to flush solids and prevent sedimentation on the V-shaped bottom 171 or on the cesspool 173 and / or pump 182. Due to the presence of this V-shaped inclined bottom 171 and a washing circuit 177, the liquid accumulated in the liquid sump 172 is constantly mixed and renewed, and thereby keeps its consistency relatively unchanged and leaves the solids in a suspended state. If necessary, the spray system 177 can be a separate circuit using a separate pump, connected for example to the inlet side of the sump 172, or can use a pump 182 connected to the recirculated circuit of the concentrated liquid described below to spray the concentrated liquid from the liquid sump 172 on the V-shaped bottom 171.

As shown in FIG. 3, the return line 180 as well as the pump 182 are used to return the liquid removed from the gas-liquid stream from the liquid sump 172 back to the concentrator 120 and thereby close the liquid recirculation loop. Similarly, a pump 184 may be installed on the inlet 186 to supply new or untreated liquid, such as landfill filtrate, through a nozzle 160 to a concentrating unit 120. One or more nebulizers 185 can also be installed inside the gas-washing unit 122 near the pleated filters 170, so that they can periodically spray clean water or a portion of the supplied wastewater onto the pleated filters 170 to rinse them.

The concentrated liquid can also be removed from the liquid sump of the gas washing unit 122 through the cesspool 173 and then further processed or disposed of appropriately in the secondary recirculation circuit 181. In particular, the concentrated liquid removed through the cesspool 173 contains a certain amount of suspended solids, which can be separated from this portion of concentrated liquid and removed from the system using secondary recirculation loop 181. For example, concentrated The liquid removed through the cesspool 173 can be fed through a secondary concentrated wastewater circuit 181 to one or more solid / liquid separation devices 183, such as a settling tank, a vibrating screen, a rotary vacuum filter, a horizontal belt vacuum filter, a belt press filter press and / or hydrocyclone. After separation of suspended solids and concentrated wastewater by the solid-liquid separator 183, a liquid portion of concentrated wastewater without solid particles can be returned to the liquid sump 172 for further processing in a primary or secondary recirculation loop connected to the concentrator.

Gas, from which liquid and suspended solids were removed when flowing through gas washing unit 122, flows through a pipe or duct from the back of gas washing unit 122 (behind corrugated filters 170) to exhaust fan 190 of exhaust unit 124 and is discharged into the atmosphere in the form of cooled gas mixed with evaporated water. Of course, an engine 192 is connected to the exhaust fan, which causes the fan 190 to create a vacuum in the gas washing unit 122 to draw gas from the torch 130 through the heat transfer pipe 140, the air pre-treatment unit 119, and the concentrating unit 120. As described above with reference to FIG. 1, an exhaust fan 190 is needed only to create a small vacuum in the gas washing unit 122 and thereby ensure proper operation of the concentrator 110.

Although the speed of the exhaust fan 190 can be changed using a device such as a variable frequency drive to create different levels of vacuum in the gas washing unit 122 and to work in a certain range of gas flow rates and even take all the gas from the torch 130, if it is not enough, it is not necessary to regulate the operation of the exhaust fan 190 in order to create a proper vacuum in the gas washing unit 122. The gas flowing through the gas washing unit 122 must have sufficient a large (minimum necessary) speed at the inlet of the gas washing unit 122. Typically, this requirement is met by maintaining a predetermined minimum pressure drop in the gas washing unit 122. But if the torch 130 does not provide the minimum required amount of gas, then increasing the speed of rotation of the exhaust fan 190 will not be able to provide the necessary pressure drop in the gas washing unit 122.

To find a way out of this situation, the cross-flow gas-washing unit 122 was equipped with a gas recirculation circuit, which can be used to supply a sufficient amount of gas to the inlet of the gas-washing unit 122 and create the required pressure drop in the gas-washing unit 122. In particular, a gas recirculation circuit contains a return line or gas channel 196, which connects the high pressure side of the exhaust unit 124 (for example, in the area behind the exhaust fan 190) with the inlet of the gas washing unit 122 (for example an example, with a gas inlet pipe of the gas-washing unit, block 122), and a damper or control mechanism 198 located in the return channel 196, which is designed to open and close the return channel 196, thereby establishing the communication of the high-pressure side of the exhaust unit 124 with the inlet pipe of the gas-washing unit 122. During operation, when the gas supply to the gas washing unit 122 is not large enough to provide the minimum required pressure drop in the gas washing unit 122, the shutter 198 (which may represent s is, for example, the gas valve or gate tambour) is open to allow direct gas from the high pressure exhaust unit 124 (i.e. the gas that passed through the exhaust fan 190) back to the inlet of the gas washing unit 122. This operation provides a sufficient amount of gas to the inlet of the gas washing unit 122 so that the exhaust fan 190 can provide the minimum required pressure drop in the gas washing unit 122.

FIG. 6 shows a particularly useful distinguishing feature of the compact fluid concentrator 110 shown in FIG. 3, which is a group of easy-opening inspection hatches 200 that can be used to penetrate the concentrator 110 for cleaning and inspection. Although FIG. 6 shows easily opening hatches 200 on one side of the gas washing unit 122, a similar group of hatches can be located on the other side of the gas washing unit 122, and a similar hatch is provided on the front side of the flooded elbow 164, as shown in FIG. As shown in FIG. 6, each of the easily opening inspection hatches 200 on the gas washing unit 122 comprises a manhole cover 202, which may be a flat metal plate suspended on the gas washing unit 122 on two hinges 204, wherein the manhole cover 202 may be closed and opened, turning on hinges 204. At the edges of the hatch cover 202 there are a lot of quickly opening locks 206 designed to fix the hatch cover 202 in the closed position and to lock the hatch cover 202 during operation of the gas washing unit 122. In an embodiment the implementation shown in Fig.6, on each manhole cover there are eight quick-opening locks 206 located around each of the manhole covers 202, although you can use any required number of such quick-opening locks 206.

7 shows one of the hatches 200 in the open position. As shown in this figure, the hatch frame 208 is raised above the wall of the gas washing unit 122 and mounted on supports 209 located between the hatch frame 208 and the outer wall of the gas washing unit 122. A gasket 210 is installed around the hole in the hatch frame 208, which may be made of rubber or other compressible material. A similar additional or main gasket can be installed around the perimeter from the inside of the hatch cover 202, to improve the quality of sealing when the hatch 200 is in the closed state.

Each quick-open latch 206, which is shown in enlarged view in FIG. 8, has a handle 212 and a latch 214 (in this case, a U-shaped metal bracket) mounted on a hinge axis 216 passed through the handle 212. The handle 212 is mounted on another hinge axis 218 mounted on the outer wall of the hatch cover 202 using the mounting bracket 219. When moving the handle 212 up and turning around the other hinge axis 218 (from the position shown in Fig. 8), the latch 214 is shifted along the outer wall of the gas washing unit 122 ( when l cover ka 202 is in the closed position), and the latch 214 can detach from the hook 220 located on the support 209, and move away from the hatch cover 202. When the handle 210 is turned in the opposite direction, the latch 214 clings to the hook 220 and attracts another hinge axis 218 and, consequently, the hatch cover 202 to the hatch frame 208. When all the fast-closing locks 206 are closed, the hatch cover 202 is pressed against the hatch frame 208, and the gasket 210 ensures their tight connection. Thus, the closure of all eight rapidly opening locks 206 on a specific hatch 200, as shown in Fig.6, provides reliable and tight closing of the hatch 200.

The use of easily opening hatches 200 replaces covers with holes and a plurality of bolts extending from the outer wall of the concentrator, which pass through these openings on the cap and are tightened with nuts to press the cap against the wall of the concentrator. Although such a bolt-and-bolt mounting mechanism, which is widely used in fluid concentrators to provide access inside the concentrator, is very reliable, it takes a lot of time and effort to remove and install the removable cover. The easy-opening hatches 200 with the quick-opening locks 206 shown in FIG. 6 can be used in this case also because since the pressure inside the gas-washing block 122 is less than the external pressure, a vacuum is created inside the gas-washing block 122, which does not need to tighten the bolts and nuts removable panel. It is understood that the configuration with hatches 200 makes it easy to open and close the hatches 200 with minimal effort and without the use of tools, and thereby provides quick and easy access to equipment inside the gas washing unit 122, such as a baffle plate 169 or replaceable filters 170, or others parts of the hub 110, which are located behind the inspection hatch 200.

As shown in FIG. 5, on the front wall of the flooded elbow 164 of the concentrating unit 120 there is also an easily opening inspection hatch 200 that provides easy access to the inside of the flooded elbow 164. However, such easily opening hatches can be located, if necessary, on any part of the fluid concentrator 110, since most of the elements of the hub 10 operate under vacuum.

The combination of features shown in FIGS. 3-8 is inherent in the compact fluid concentrator 110, which uses the waste heat of gas from flaring gas from organic waste, waste heat that would otherwise be emitted directly into the atmosphere. It is important to note that the concentrator 110 uses only the minimum amount of expensive material with high temperature resistance for the manufacture of pipes and construction equipment necessary for working with high-temperature gases leaving the torch 130. In particular, the length of the heat transfer pipe 140, which is made of the most expensive materials , minimized, which reduces the cost and weight of the fluid concentrator 110. In addition, due to the small size of the heat transfer pipe 140, only a minimum the number of scaffolds in the form of a support rack 142, which further reduces the cost of constructing a hub 110. In addition, the air pre-treatment unit 119 is located directly on the concentrating unit 120 and the gas in these blocks flows from top to bottom, which allows these hub units 110 to be installed directly on ground or skid. Further, this configuration allows the hub 110 to be placed very close to the torch 130, which makes it more compact. Similarly, this configuration allows the high-temperature units of the concentrator 110 to be placed (for example, the upper part of the flame 130, the heat transfer pipe 140 and the air pre-treatment unit 119) above the ground, and there is no need to fear accidental contact, which leads to a higher level of safety. In fact, due to the rapid cooling that occurs in the section with the venturi profile 162 of the concentrating unit 120, both the section with the venturi profile 162 and the flooded elbow 164 and the gas washing unit 122 are usually cooled sufficiently so that they can be touched without being afraid to burn themselves (even if the gas leaving the torch 130 had a temperature of 1800 ° F). Rapid cooling of the gas-liquid mixture allows the use of materials of lower cost, which are easier to manufacture and which have corrosion resistance. In addition, components after the submerged elbow 164, such as the gas washing unit 122, the exhaust fan 190 and the exhaust unit 124, can be made of materials such as fiberglass.

The fluid concentrator 110 is also a very fast concentrator. As the concentrator 110 is a direct contact concentrator, it is not at risk of sedimentation, clogging or clogging to the extent that is inherent in most other concentrators. Further, the ability to regulate the operation of the torch by opening and closing the torch cap 134 allows the torch 130 to be continuously used to burn gas from organic waste, regardless of whether the hub 110 is operating or not, without stopping its operation during start-up and stop of the hub 110. In particular, flare cap 134 can be quickly opened at any given time so that flare 130 can simply burn gas from organic waste, as it usually does when the hub 110 is turned off. On the other hand, the flare cap can but quickly close the concentrator 110 at the time of start-up and thereby direct all hot gases generated in the torch 130 to the concentrator 110, which allows the concentrator 110 to start working without stopping the torch 130. In any case, the concentrator 110 can be started and stopped, changing only the position of the torch cap 134, but not stopping the operation of the torch 130.

If necessary, during operation of the concentrator 110, the flare cap 134 can be partially opened to control the amount of gas supplied from the torch 130 to the concentrator 110. This gas flow control in combination with the regulation of the atmospheric air inlet valve can be used to control the gas temperature at the inlet of venturi profile 162.

In addition, due to the compact configuration of the air pre-treatment unit 119, the concentrating unit 120 and the gas-washing unit 122, the individual parts of the concentrating unit 120, the gas-washing unit 122, the exhaust fan 190 and at least the lower part of the exhaust unit 124 can be permanently installed (attach and use as a support) on the slide or plate 230, as shown in figure 2. The upper part of the concentrating unit 120, the air pre-treatment unit 119 and the heat transfer pipe 140, as well as the upper part of the exhaust pipe can be removed and laid on a slide or on a stove 230 during transportation or they can be transported in a separate truck. Due to the fact that the lower parts of the hub 110 can be mounted on a slide or plate, the hub 110 is easy to remove and install. In particular, during the installation of the hub 110 of the slide 230, on which the gas washing unit 122 is mounted, the flooded elbow 164 and the exhaust fan 190 can be unloaded at the place where the hub should be used, simply unloading them from the slide 230 to the ground or to another storage the area on which the hub 110 will be assembled. After that, a section with a Venturi profile 162, a cooler 159 and an air pre-treatment unit 119 can be placed on top and attached to the flooded elbow 164. Then, the pipe 150 can be extended so that it matches the height of the torch 130 to which a hub 110 should be connected. In some In cases, it may be necessary to first install the flare-cap block 132 to the already existing flare 130. After that, you can raise the heat transfer pipe 140 to an appropriate height and fasten between the flare 130 and the block for preliminary air treatment 119, replacing the support strut 142. For concentrators with an evaporation capacity of 10,000 to 30,000 gallons per day, it is possible that the entire flare assembly 115 is mounted on the same skid or plate 230 on which the concentrator 120 is mounted.

Since most pumps, pipes, sensors, and electronic equipment are located or connected to a concentrating unit 120, a gas washing unit 122, or an exhaust pump 190, installing a concentrator 110 at a specific location does not require a large number of pipes and electrical work at the installation site. As a result, the hub 110 can be relatively easily installed and mounted (or dismantled and disassembled) at a specific location. In addition, since most of the components of the hub 110 are permanently mounted on a slide 230, the hub 110 can easily be transported by truck or other vehicles and can easily be unloaded and installed at a specific location, such as a site near the torch in a landfill.

FIG. 9 shows a control circuit 300 that can be used for the hub 110 of FIG. 3. As shown in FIG. 9, the control system 300 comprises a controller 302, which may be a controller such as a digital signal processor, a programmable logic controller, which may, for example, provide control based on multi-stage logic, or some other type of controller. The controller 302 is connected, of course, to the various components in the hub 110. In particular, the controller 302 is connected to the drive motor 135 of the flare cap 134, which opens and closes the flare cap 134. The drive motor 135 can be used to adjust the position of the flare cap 134 by moving it between fully open and fully closed positions. But if necessary, the controller 302 can adjust the drive motor 135 so that it moves the flare cap 134 to any of a variety of intermediate positions ranging from a fully open position to a fully closed position. If necessary, the engine 135 can continuously move the flare cap 134, setting at any desired point between the fully open and fully closed positions.

In addition, the controller 302 is connected to the intake valve of atmospheric air 306 located in FIG. 3 in the air pre-treatment unit 119 in front of the section with the venturi profile 162, and can be used to control pumps 182 and 184, which regulate the size and ratio of the injection of new liquid, received at the concentration and recycled liquid, which was processed in the concentrator 110. The controller 302 can be connected to a level sensor 317 in the liquid sump (for example, to a float sensor, non-contact at the sensor, such as radar or acoustic sensor, or differential pressure sensor). The controller 302 may use the signal from the level sensor 317 in the liquid sump to control pumps 182 and 184 and maintain the level of concentrated liquid in the liquid sump 172 corresponding to a predetermined or desired value. The controller 302 can also be connected to an exhaust fan 190 to control the operation of the exhaust fan 190, which may be a single speed fan, a variable speed fan, or a continuously variable speed fan. In one embodiment, the drive for the exhaust fan 190 is a variable frequency motor, the frequency of which is changed to adjust the fan speed. In addition, the controller 302 is connected to a temperature sensor 308 located, for example, at the inlet of the concentrating unit 120 or at the input of the section with the venturi profile 162, and receives a temperature signal generated by the temperature sensor 308. The temperature sensor 308 may also be located behind the section with the venturi profile 162, or the temperature sensor 308 may include a pressure sensor generating a pressure signal.

During operation and, for example, when starting up the concentrator 110, when the torch 130 continues to work and thus burns gas from organic waste, the controller 302 must first turn on the exhaust fan 190 to create a vacuum in the gas washing unit 122 and the concentrating unit 120. After that or at the same time, the controller 302 sends a signal to the engine 135 to close the flare cap 134 partially or completely and to direct the waste heat from the flare 130 to the heat transfer pipe 140, and therefore to the air pre-treatment unit 11 9. Receiving a temperature signal from temperature sensor 308, controller 302 can adjust the atmospheric air inlet valve 306 (usually closing it partially or completely) and / or the flare cap actuator to adjust the gas temperature at the inlet of the concentrating unit 120. Generally speaking, the atmospheric inlet valve air 306 may be brought into a fully open position by a biasing member, such as a spring (i.e., it may be a normally open valve), and controller 302 may begin to close valve 306 to adjust the amount of GUT atmospheric air entering the air handling unit pre-119 (by creating a vacuum in the air pre-processing block 119) and thereby bring the mixture of air and hot gases from the torch 130 to a desired temperature. If necessary, the controller 302 can also adjust the position of the flare cap 134 (by setting it to any position between the fully open and fully closed positions) and can change the speed of the exhaust fan 190 to control the amount of gas entering the air pre-treatment unit 119 from the torch 130. It is clear that the amount of gas flowing through the concentrator 110 can be changed, for example, depending on the temperature and humidity of the atmospheric air, the temperature of the flare gas, or the amount of gas leaving the torch 130. Consequently, the controller 302 can control the temperature and amount of gas flowing through the concentrating unit 120 by changing one or more parameters, including the degree of closure of the atmospheric air inlet valve 306, the position of the flare cap 134, and the exhaust speed fan 190, for example, based on the measurement of the temperature sensor 308 at the inlet of the concentrating unit 120. This feedback system is necessary because in many cases the air leaving the torch 130, and EET temperature ranging from 1200 ° F to 1800 ° F, which is too large or exceeds that value which it should have to ensure efficient operation of the hub 110.

In any case, as shown in FIG. 9, the controller 302 can also be connected to an engine 310, which can change the position of the venturi plate 163 in the narrowed portion of the concentrating unit 120 to adjust the level of turbulence created by the concentrating unit 120. And the controller 302 can monitor the operation of pumps 182 and 184 in order to change the speed (and the ratio of speeds) at which the pumps 182 and 184 supply circulating fluid and new waste water to the inlets of the cooler 159 and the section with the venturi profile 162. In one embodiment, the troller 302 can adjust the ratio of the circulating fluid to the new fluid at 10: 1, so that if the pump 184 supplies the new fluid to the inlet 160 at a speed of 8 gallons per minute, then the recirculation pump 182 delivers the concentrated fluid at a speed of 80 gallons per minute. Instead or additionally, the controller 302 can adjust the flow rate of the new fluid sent to the concentrator for processing (pump 184), maintaining the amount of concentrated fluid in the fluid sump 172 at the same or predetermined level, for example, using a level sensor 317. Of course , the amount of liquid in the liquid sump 172 will depend on the concentration rate in the concentrator, the speed at which the concentrated liquid is pumped out by the pump, or fed into the liquid sump 172 toricity recirculation loop and the speed at which the pump 182 delivers fluid from the fluid sump 172 in the hub the primary recirculation loop.

If necessary, the atmospheric air inlet valve 306 or the flare cap 134, separately or together, may be in a safety open position such that the flare cap 134 and the air inlet valve 306 open in the event of a system malfunction (for example, a control signal is missing) or shutdown of the hub 110. In one case, the flare cap motor 135 may be spring loaded or pushed out by a squeezing member such as a spring to hold the flare cap 134 open positioning or to ensure that the flare cap 134 is opened after the engine 135 is de-energized. Alternatively, the squeezing element can be a counterweight 137 to the flare cap 134, which can be positioned so that the flare cap 134 itself goes into the open position under the influence of the counterweight 137 when the engine 135 The control signal is de-energized or disappears. As a result, the flare cap 134 quickly opens when power is cut off or when the controller 302 opens the flare cap 134, allowing hot gas to exit the flare 130 through the top opening. Of course, other methods can be used to move the flare cap 134 to the open position in the absence of a control signal, including using a torsion spring on the hinge axis 136 of the flare cap 134, a hydraulic or pneumatic system that raises the pressure in the cylinder to close the flare cap 134 and when the pressure in the cylinder decreases, the flare hood 134 opens in the absence of a control signal.

According to the above, the flare cap 134 and the atmospheric air inlet valve 306 act synchronously, protecting the structural materials used in the hub 110 and, as soon as the system is turned off, the flare cap 134 and the atmospheric air inlet valve 306 automatically open, which thereby do not allow hot gas generated in the flare 130, to penetrate into the concentrator 110 and at the same time allow atmospheric air to cool the concentrator 110.

In addition, the atmospheric air inlet valve 306 can be similarly spring-loaded or otherwise pressed so that it opens when the hub 110 is turned off or if there is no control signal supplied to the valve 306. Due to this, the air pre-treatment unit 119 and the concentration unit 120 are quickly cooled through open flare cap 134. In addition, by quickly opening the atmospheric air valve 306 and flare cap 134, the controller 302 can quickly shut down the hub 110, not from lyuchaya or without affecting the operation of the torch 130.

Further, as shown in FIG. 9, the controller 302 can be connected to a venturi plate motor 310 or some other drive that rotates or sets the venturi plate 163 at a certain angle in a portion with a venturi profile 162. With a motor 310, the controller 302 can change the angle of the venturi plate 163 to regulate the gas flow rate through the concentrating unit 120 and thereby change the nature of the turbulent gas flow flowing through the concentrating unit 120, achieving better mixing of liquid with gas in it and More complete evaporation of the liquid. In this case, the controller 302 can change the speed of the pumps 182 and 184 and at the same time change the slope of the venturi plate 163 to achieve optimal concentration of wastewater. It is understood that in this way, the controller 302 can coordinate the position of the venturi plate 163 with the position of the flare cap 134, the position of the intake valve of atmospheric air 306 and the speed of the exhaust fan 190 to maximize the degree of concentration (turbulent mixing) of the wastewater, avoiding the complete evaporation of water and thereby preventing the formation of solid particles. Controller 302 may use the pressure input from pressure sensors to select the position of the venturi 163. Of course, the venturi 163 can be adjusted either manually or automatically.

The controller 302 can also be connected to an engine 312 that controls the operation of the shutter 198 in the gas recirculation circuit of the gas washing unit 122. The controller 302 can cause the engine 312 or other type of actuator to move the shutter 198 from the closed position to the open or partially open position, for example, by signals from pressure sensors 313, 315 located at the inlet and outlet of the gas from the gas washing unit 122. The controller 302 may set the damper 198 to a position in which gas is supplied from the high pressure side of the exhaust unit and 124 (behind the exhaust fan 190) to the inlet of the gas washing unit to maintain a predetermined minimum pressure drop between the two pressure sensors 313, 315. Maintaining a minimum pressure drop ensures proper operation of the gas washing unit 122. Of course, the damper 198 can be manually controlled or electrically controlled .

Thus, from the foregoing, it follows that the controller 302 can create one or more closed / open control loops used to start or stop the hub 110 without disrupting the operation of the torch 130. For example, the controller 302 can create a control loop for the flare cap that opens or closes flare hood 134, an air valve control circuit that opens or starts to open an atmospheric air intake valve 306, and an exhaust fan control circuit that starts the sludge and stops the exhaust fan 190 depending on whether the hub 110 starts or stops. In addition, during operation, the controller 302 can create one or more real-time control loops that can control the various elements of the hub 110 separately or in combination with each other to improve or optimize the concentration method. By creating these real-time control loops, controller 302 can control the speed of the exhaust fan 190, the position or angle of the venturi plate 163, the position of the flare cap 134, and / or the position of the shut-off element of the intake valve of atmospheric air 306 to control the flow rate of the fluid flowing through the concentrator 110, and / or the air temperature at the inlet to the concentrating unit 120 based on signals from temperature and pressure sensors. In addition, the controller 302 can provide the performance of the method of concentration in stationary conditions by regulating the pumps 184 and 182, which feed the new and circulating fluid to the concentrating unit 120. And the controller 302 can create a pressure control loop to adjust the position of the shutter 198 and provide proper operation of the gas washing unit 122. Of course, although the controller 302 is shown in FIG. 9 as a single control device that creates different control loops, the controller 302 may represent many different control devices, for example, many different programmable logic controllers.

It is understood that the concentrator 110 proposed here directly utilizes hot gas emissions in process methods after these gas emissions have been carefully processed to meet the requirements of gas emission standards, and thus unconditionally meet the operational requirements of a method that generates waste heat, and a method that uses waste heat in a simple, reliable and efficient way.

In addition to being an important component of the hub 110 during its operation, the flare hood 134 with automatic or manual drive described here can be used in stand-alone operation to provide weather protection to the torch itself or the torch-hub assembly when the torch is not operating . Closed by a flare cap 134, the internal equipment of the metal housing of the torch 130 together with its lining, burners and other important components of the flare unit 115 and heat transfer unit 117 is protected from corrosion and general wear associated with exposure to these components. In this case, the controller 302 can control the engine 135 of the flare cap 134, setting it in a fully open or partially open state during operation of the torch 130 at idle. Furthermore, in addition to using the torch cap 134, which automatically closes when the torch 130 is turned off, and automatically opens when the torch 130 is lit, a small burner, such as a conventional pilot light, can be installed inside the torch 130, which can burn when the torch 130 is turned off and flare cap 134 is closed. This small burner further contributes to protection against wear of the flare components due to moisture, as it will keep the internal equipment of the torch 130 dry. An example of an autonomous torch that can use the torch cap 134 described here when operating autonomously is an autonomous torch mounted in a landfill to control the gas content in the air when a power plant operating on gas from organic waste is turned off.

Although the liquid concentrator 110 has been described above connected to a torch for burning gas from organic waste in order to use the waste heat from this torch, the liquid concentrator 110 can easily be connected to other sources of waste heat. For example, FIG. 10 shows a fluid concentrator 110 of such a design that it can be connected to the exhaust pipe of a power plant 400 with internal combustion engines and use the waste heat of the engines to concentrate wastewater. Although in one embodiment, an engine in a power plant 400 can run on organic waste gas to generate electricity, the hub 110 can also be connected to the exhaust pipe of other types of engines, including engines of this type that run on gasoline or diesel fuel.

10, the exhaust gases generated in an engine (not shown in the figure) at a power plant 400 enter a muffler 402 outside the power plant 400, and from there, to an exhaust pipe 404 provided with an exhaust cap 406 on top. The cap 406 is provided with a counterweight so that it can close the exhaust pipe 404 when there are no exhaust gases in the pipe 404, but was easily opened by the exhaust gases and the pipe 404. In this case, the exhaust pipe 404 has a Y-shaped connector designed to connect the pipe 408 to the heat transfer pipe 408, koto A swarm exhaust gas (waste heat source) enters the expansion section 410 from the engine. The expansion section 410 is coupled to the cooler 159 of the concentrator 110 and directs the exhaust gas from the engine directly to the concentrating unit 120 of the concentrator 110. When using the exhaust gases of the engine as a source of waste heat, it is not necessary to install an atmospheric air inlet valve in front of the concentrating unit 120, since the exhaust gas at the engine outlet usually has a temperature of less than 900 ° F, so that no GSI it strongly cooled prior to entering the chiller 159. The remaining portion of the concentrator 110 are the same as described above with reference to Figures 3-8. As a result, it can be seen that the fluid concentrator 110 can be easily adapted to use a wide variety of waste heat sources without making significant design changes.

Typically, when controlling the fluid concentrator 110 shown in FIG. 10, the controller turns on the exhaust fan 190 while the engine at the power plant 400 is running. The controller increases the speed of the exhaust fan 190 from a minimum value until most or all of the exhaust gases go from the pipe 404 to the heat transfer pipe 408 instead of leaving the exhaust pipe 404 to the atmosphere. It is not difficult to determine when such an operating mode will be achieved, it corresponds to the moment when, with an increase in the speed of the exhaust fan 190, the hood 406 first sits on top of the exhaust pipe 404. It is important not to allow a further increase in the speed of the exhaust fan 190 at which a more than necessary mode is created , vacuum in the hub 110, and thereby ensure that the operation of the hub 110 does not lead to a change in backpressure and, in particular, to the creation of undesirable levels of leakage experienced by the engine on the electric Rostan 400. Changing the back pressure or creating a suction in the exhaust pipe 404 may adversely affect the combustion of fuel in the engine, which is undesirable. In one embodiment, a controller (not shown in FIG. 10), such as a programmable logic controller, may use a pressure sensor installed in a pipe 404 near cap 406 to constantly monitor pressure at that location. The controller can then provide a signal to the variable frequency drive on the exhaust fan 190 to control the speed of the exhaust fan 190, maintain the pressure at a predetermined level, and thereby ensure that unwanted backpressure or suction does not affect the engine.

11 and 12 show a cross section in side view and a cross section in top view of yet another embodiment of a fluid concentrator 500. The concentrator 500 is mounted in a vertical position. However, the hub 500 shown in FIG. 11 may be located in a horizontal position or in a vertical position, depending on the specific limitations imposed when used for a specific purpose. For example, a truck-mounted hub modification may be horizontal so that the hub can pass under bridges and overpasses during transportation from one place to another. The fluid concentrator 500 has a gas inlet 520 and a gas outlet 522. The gas inlet 520 and the gas outlet 522 are connected by a flow channel 524. The flow channel 524 has a narrowed portion 526 that accelerates the flow of gas through the flow channel 524. Before the narrowed section 526, liquid is injected into the gas stream. through the pipe 530. In contrast to the embodiment shown in FIG. 1, in the embodiment shown in FIG. 11, the constricted portion 526 directs the gas-liquid mixture into the cyclone chamber 551. Cyclical to Amer 551 enhances the mixing of gas and liquid, while at the same time acting as the mist eliminator shown in FIG. the gas-liquid mixture enters tangentially into the cyclone chamber 551 (see FIG. 12), and then moves through the cyclone chamber 551 like air in the cyclone in the direction of the liquid removal section 554. The cyclonic swirl is amplified by the hollow cylinder 556 located in the cyclone chamber 551, through which gas enters the gas outlet 522. The hollow cylinder 556 is a physical barrier that provides cyclone swirl throughout the cyclone chamber 551, including at the liquid outlet 554.

When the gas-liquid mixture passes through the narrowed portion 526 of the flow channel 524 and circulates in the cyclone chamber 551, part of the liquid is vaporized and absorbed by the gas. Then, the centrifugal force accelerates the movement of the gas droplets carried away by the gas towards the side wall 552 of the cyclone chamber 551, where the carried away droplets of liquid merge to form a film on the side surface 552. At the same time, the centripetal forces created by the exhaust fan 550 collect gas released from the droplets at the inlet 560 of the cylinder 556 and directing it into the gas outlet 522. Thus, the cyclone chamber 551 acts both as a mixing chamber and as a mist collecting chamber. When a liquid film flows in the chamber in the direction of the liquid outlet 554 under the combined action of gravity and swirl in the cyclone chamber 551 in the direction of the liquid outlet 554, the gas constantly circulating in the cyclone chamber 551 also evaporates part of the liquid film. When the liquid film drains into the liquid withdrawal portion 554 from the cyclone chamber 551, the liquid enters the recirculation loop 542. In a similar manner, the liquid circulates through the concentrator 500 until the desired degree of concentration is achieved. Part of the concentrated sludge can be taken through the cesspool 546 when the sludge reaches the desired level of concentration (this method is called purging). Fresh liquid is introduced into the circuit 542 through the inlet pipe 544 of fresh liquid with a speed equal to the sum of the evaporation rate and the rate of removal of sludge through the cesspool 546.

When the gas circulates in the cyclone chamber 551, it is cleaned of liquid droplets and moves in the direction of the liquid outlet section 554 of the cyclone chamber 551 by the action of the exhaust fan 550 and in the direction of the inlet 560 of the hollow pipe 556. Then, the purified gas enters the hollow pipe 556 and finally, it is discharged through the gas outlet 522 into the atmosphere or sent for further processing (for example, for oxidation in a flare).

13 is a diagram of a distributed liquid concentrator 600 having such a configuration that allows the use of a concentrator 600 with a variety of different types of waste heat sources, even waste heat sources located in places that are difficult to access, for example, on the sides of buildings, among different types of other equipment, away from roads or other access routes. Although the liquid concentrator 600 described herein is used to treat and concentrate a filtrate, such as a filtrate collected in a landfill, a liquid concentrator 600 can be used to concentrate other types of liquids, including many different wastewaters.

Generally speaking, the fluid concentrator 600 comprises a gas inlet 620, a gas outlet or gas exhaust 622, a flow passage 624 extending from the gas inlet 620 to the gas exhaust 622, and a liquid recirculation system 625. The concentrator block comprises a flow passage 624 that includes a cooling section 659 including a gas inlet pipe 620 and a liquid inlet pipe 630, a section with a venturi profile 626 located behind the cooling section 659, and a discharge or exhaust fan 650 are connected downstream of the venturi section 626. A fan 650 and a flooded elbow 654 connect a gas outlet pipe of the concentrating unit (for example, the exhaust nozzle of a section with a venturi profile 626) to conduit 652. In this case, the flooded elbow 654 rotates the flow channel 624 by 90 degrees. If necessary, the flooded elbow 654 can provide rotation at an angle that is less than or greater than 90 degrees. The pipeline 652 is connected to a mist eliminator, shown in this case in the form of a cross-flow gas-washing apparatus 634, which, in turn, is connected to a chimney 622A having a gas exhaust hole 622.

The recirculation system 625 includes a liquid sump 636 connected to the liquid outlet of the cross-flow gas washer 634, and a recirculation pump 640 connected between the liquid sump 636 and the conduit 642 that supplies the circulating liquid to the liquid inlet 630. The feeder 644 also supplies the filtrate or other the liquid to be treated (for example, concentrated liquid) in the liquid inlet 630 so that it enters the cooler 659. The recirculation system 625 contains akzhe fluid outlet 646 connected to conduit 642 which delivers a quantity of the circulating fluid (or concentrated liquid) into the reservoir 649 for storage, recycling and sedimentation. Heavier or more concentrated portions of the liquid in the settling tank 649 are lowered to the bottom of the tank 649 in the form of sludge, which is removed and transported in order to be removed in concentrated form. Less concentrated portions of the liquid from the reservoir 649 are fed back to the liquid sump 636 for reprocessing and further concentration, as well as to ensure that the liquid inlet 630 is properly fed into the inlet at any time and thereby prevent the formation of dry particles. Dry particles can form with a reduced ratio of the volume of the processed fluid to the volume of hot gas.

During operation, the cooler 659 mixes the fluid from the fluid inlet 630 with waste heat gas collected, for example, from an engine muffler and exhaust pipe 629 associated with an internal combustion engine (not shown in the figure). The fluid from the fluid inlet valve 630 may be, for example, a filtrate to be treated or concentrated. As shown in FIG. 13, the cooler 659 is connected in a vertical position above the section with the venturi profile 626, which contains a narrowed section that accelerates the flow of gas and liquid through the flow channel 624 immediately after the section with the venturi profile 626 and in front of the fan 650. Of course, the fan 650 serves to create a vacuum directly behind the section with the Venturi profile 626, sucking gas from the exhaust pipe 629 through the section with the Venturi profile 626 and the flooded elbow 654 to provide mixing of gas and liquid.

As indicated above, the cooler 659 receives hot exhaust gas from the exhaust pipe 629 of the engine and can be connected directly to any desired portion of the exhaust pipe 629. In this illustrative embodiment, the exhaust pipe 629 of the engine is installed outside the building 631, in which there are one or more generators that produce electricity using gas from organic waste as fuel. In this case, the cooler 659 may be connected directly to a steam trap (e.g., a condensation pot) connected to the exhaust pipe 629 (i.e., to the bottom of the exhaust pipe 629). Here, cooler 659 can be installed directly below or near the pipe 629, so it will take only a few inches or at most several feet of an expensive pipe of high temperature resistant material to join them together. But if necessary, the cooler 659 can be connected to another section of the exhaust pipe 629, for example, to the top or to the middle part of the pipe 629 through the corresponding elbow or branch.

As indicated above, through the inlet pipe 630, the liquid to be evaporated (for example, landfill filtrate) is injected into the flow channel 624 through a cooler 659. If necessary, the liquid inlet pipe 630 may include a replaceable nozzle for spraying liquid in the cooler 659. The liquid inlet pipe 630, regardless of whether it is equipped with a nozzle or not, it can introduce fluid in any direction, both perpendicular to the gas flow and parallel to the gas flow moving through the flow channel 624. In addition, when the gas (and waste heat, contained in it) and the liquid pass through the area with the Venturi profile 626, according to the Venturi principle, the flow velocity increases and a turbulent flow is formed, which completely mixes the gas and liquid in the flow channel 624 immediately after the section with the Venturi profile 626. As a result of mixing in the turbulent mode, part The liquid evaporates quickly and is part of the gas stream. A large amount of thermal energy from the waste heat is spent on evaporation to increase the latent heat, which is removed from the concentration system 600 in the form of water vapor in the exhaust gas.

From the section with the Venturi profile 626, the gas-liquid mixture enters the flooded elbow 654, where the flow channel 624 rotates at an angle of 90 degrees, changing the vertical direction of the flow to the horizontal direction of the flow. the gas-liquid mixture flows around the fan 650 and enters the high-pressure region on the discharge side of the fan 650, the high-pressure region being in the pipeline 652. The use of the flooded elbow 654 at this point in the system is necessary for at least two reasons. Firstly, the liquid in the lower part of the flooded elbow 654 reduces erosion at the turning point of the flow channel 624, which usually occurs under the action of particles suspended in a gas-liquid mixture, which would enter a 90-degree bend at high speed and would strike at a sharp angle the lower surface of a normal knee, if the flooded knee 654 were not used. The liquid in the lower part of the flooded knee 654 absorbs the energy of these particles and thus protects the lower surface of the flooded knee 654 from erosion. In addition, liquid droplets still contained in the gas-liquid mixture in the flooded knee merge much more easily and are removed from the stream if they hit the liquid. That is, the liquid at the bottom of the flooded elbow 654 is used to trap liquid droplets hitting it, since the liquid droplets contained in the stream are much more easily retained if these atomized liquid droplets come in contact with the liquid. Thus, the flooded elbow 654, which may have a fluid outlet (not shown), for example, into the recirculation circuit 625, serves to remove some of the droplets of the treated liquid and condensate from the gas-liquid mixture leaving the area with the Venturi profile 626.

It should be noted that the gas-liquid mixture flowing along the section with the Venturi profile 626 quickly approaches the adiabatic saturation point, which is at a temperature that is much lower than the gas temperature at the outlet of the exhaust pipe 629. For example, although gas may exit the exhaust pipe 629 have a temperature in the range of 900 ° F to 1800 ° F, the gas-liquid mixture in all sections of the concentration system 600 behind the section with the Venturi profile 626 will usually have a temperature in the range of 150 ° F to 190 ° F, although the temperature of the mixture may be above and below this temperature range depending on the operating parameters of the system. As a result, sections of the concentration system 600 behind the section with a Venturi profile 626 do not need to be made of heat-resistant materials and do not need to be insulated at all or can be insulated only to the extent necessary for the transportation of gases with elevated temperature, if the insulation is carried out in order to more fully utilize waste heat contained in hot gas. And also sections of the concentration system 600 behind the section with the Venturi profile 626 located in such places, for example, laid on the surface of the earth where people can come into contact with them, do not pose a significant danger or need only minimal external protection. In particular, the areas of the concentration system behind the area with the Venturi profile 626 can be made of fiberglass and may need only minimal insulation or not at all. It should be noted that the gas-liquid flow can be supplied through the sections of the concentration system behind the section with the Venturi profile 626 over a relatively large distance, while still remaining near the adiabatic saturation point, and thereby allowing it to be easily transported via pipeline 652 from building 631 to a more accessible place, in wherein other equipment associated with the hub 600 may be housed in a conventional manner. In particular, the portion of pipeline 652 may extend 20 feet, 40 feet, or even an even greater distance, although the flow still remains in a state close to adiabatic saturation. Of course, these distances can be more or less depending, for example, on the ambient temperature, the type of pipeline used or the presence of insulation. In addition, since the portion of conduit 652 is located on the high pressure side of the fan 650, it is easy to remove condensate from this stream. In the embodiment shown in FIG. 13, a portion of conduit 652 is shown enveloping an air cooler or passing under an air cooler associated with engines inside building 631. But the air cooler in FIG. 13 is just one variant of those obstructions that may occur near building 631 and which do not allow to place all components of the concentrator 600 near the source of waste heat (in this case, near the exhaust pipe 629). Other obstacles may be other equipment, vegetation, such as trees, other buildings, inaccessible territory without roads and convenient approaches.

In any case, the portion of the pipeline 652 directs the gas-liquid flow in a state close to the adiabatic saturation point to the mist eliminator 634, which may be, for example, a cross-flow gas-washing apparatus. A mist eliminator 634 serves to remove entrained droplets of liquid from the gas-liquid stream. The separated liquid is collected in the liquid sump 636, from where it enters the pump 640. The pump 640 delivers the liquid through the return line 642 of the recirculation circuit 625 to the liquid inlet 630. Thus, the entrained liquid can continue to be concentrated by evaporation to the desired concentration level and / or fed in order to prevent the formation of dry particles. Fresh liquid enters the concentration through the inlet pipe of fresh liquid 644. The rate of supply of fresh liquid to the recirculation circuit 625 should be equal to the sum of the rate of evaporation of the liquid when the gas-liquid mixture passes through the flow channel 624 and the rate of withdrawal of liquid or sludge from the settling tank 649 (provided that the level fluid in the settling tank 649 does not change). In particular, part of the liquid can be discharged through the cesspool 646 when the liquid in the recirculation loop 625 reaches the desired degree of concentration. Part of the liquid discharged through the cesspool 646 can be sent to the settling tank 649 for storage, where the concentrated liquid is allowed to settle and is separated into its constituent components (for example, the liquid part and the semi-solid part). The semi-solid part can be removed from tank 649 and removed or further processed.

As indicated above, the fan 650 sucks gas through one section of the flow channel 624, which is under vacuum, and pumps gas through another section of the flow channel 624, which is under high pressure. Cooler 659, a venturi section 626, and a fan 650 can be attached to building 631 using any type of connecting device and can be in close proximity to the waste heat source. However, the mist eliminator 634 and the gas outlet pipe 622, as well as the settling tank 649, may be located at some distance from the cooler 659, a section with a Venturi profile 626 and fan 650, for example, in an easily accessible place. In one embodiment, a mist eliminator 634 and a gas outlet 622, as well as a settling tank 649, may be mounted on a movable platform, such as a liquid sump or trailer frame.

Figures 14-16 show another embodiment of a fluid concentrator 700 that can be mounted on a fluid sump or trailer frame. In one embodiment, some components of the concentrator 700 may remain on the frame and used to concentrate the fluid in this position, while other components can be removed and installed near the waste heat source in the manner shown in the embodiment of FIG. 13. The fluid concentrator 700 has a gas inlet 720 and a gas outlet 722. The gas inlet 720 communicates with the gas outlet 722 through the flow channel 724. The flow channel 724 has a narrowed section or a section with a Venturi profile 726, which increases the gas flow rate through the flow channel 724. The gas is sucked in to cooler 759 by an exhaust fan (not shown in the figures). Liquid is injected into the gas stream in cooler 759 through a fluid inlet 730. Gas flows from a section with a Venturi profile 726 to a mist eliminator (or cross-flow gas scrubber) 734 through an elbow 733. From the mist eliminator 734, gas enters a gas outlet 722 through a pipe 723. Of course, as mentioned above, some of these components can be removed from the frame and installed directly next to the waste heat source, while other components (such as a mist eliminator 734, pipe 723 and gas outlet 722) may remain on the frame.

When the gas-liquid mixture passes through section 726 with the Venturi profile of the flow channel 724, part of the liquid is vaporized and absorbed by the gas, spending most of the thermal energy from the waste heat to increase the latent heat, which is removed from the concentration system 700 in the form of water vapor in the exhaust gas.

In the embodiment shown in FIGS. 14-16, portions of the fluid concentrator 700 can be dismantled and mounted on the fluid sump or trailer of the truck for transportation. For example, cooler 759 and a venturi section 726 can be removed from elbow 733, as shown in FIG. 14 by a dashed line. Similarly, you can remove the pipe 723 from the fan 750, as shown in Fig.14 dashed line. Elbow 733, mist eliminator 734 and exhaust fan 750 can be attached to the liquid sump or trailer of the truck 799 as a whole. The pipe 723 can be mounted separately to the liquid sump or trailer of the 799 truck. The cooling section 759 and the section with the Venturi profile 726 can also be mounted on a pallet or trailer of the truck 799 or transported separately. The block design of the fluid concentrator 700 simplifies its transportation.

Various changes can be made to the applications of devices and methods described herein to improve the removal of pollutants from concentrated wastewater and from the exhaust gas used to concentrate these wastewaters. Such changes can be especially useful where contaminants intended for disposal are found along with substances that are normally regulated by government agencies. Examples of such pollutants are sulfur oxides (SOx), which are usually present in the exhaust gas from the combustion of gas from organic waste, as well as ammonia (NH ₃ ). The following is a description of the changes that can be made to the applications of the devices and methods described above to ensure the removal of SOx and NH ₃ , but this description should not be limited to the removal of only these contaminants.

SOx Removal

Hydrogen sulfide (H ₂ S) is a known poisonous gas that can be released during bacterial decomposition (chemical reduction) of compositions containing sulfur, sulfites and sulfates, and present in landfill waste. After formation, H ₂ S combines with other gases generated due to the bacterial action of all species occurring in the landfill, resulting in the formation of gas from organic waste. In general, the greater the amount of waste containing sulfur, sulfites and sulfates, the greater the expected amount of hydrogen sulfide. For example, the waste may contain sulfates, the source of which is calcium sulfate (for example, gypsum wallboard material), the contribution of which is 10,000 parts of H ₂ S per million parts (wt.) Of gas from organic waste. Hydrogen sulfide is a component of gas from organic waste burned in a flare plant in a landfill, as described in this document, for example. Combustion of H ₂ S in a gas flare, reciprocating engine or turbine is preferred to convert H ₂ S to sulfur oxides (SOx), avoiding the costly pretreatment of gas from organic waste to remove H ₂ S. However, sulfur oxides in some countries may regarded as an air pollutant. Another advantage of H ₂ S combustion in a flare is that H ₂ S increases the amount of heat in the flare exhaust, which can be used to concentrate landfill filtrate, reducing the total amount of fuel required.

Wet scrubbers are typically used to remove SOx from the exhaust gases generated by the combustion of fuels that contain sulfur compounds, including H ₂ S. Examples of such scrubbers include spray and packing columns contacting (wet contact) with alkaline materials (e.g. solutions or catalyzed suspensions) sodium hydroxide or lime (CaCO ₃ )) directly with an exhaust gas designed to “purify” (ie remove) SOx from it. The principle behind wet cleaning can be used in the context of the wastewater concentrator described in this document.

A known concentration of alkaline material can be added to the wastewater in an amount sufficient to react with SOx present in the exhaust gas and convert it to sodium hydroxide and sodium sulfate (in which alkali is NaOH) and calcium sulfate (CaSO ₄ ), in which alkali is lime. After formation, salts of sodium sulfite / sodium sulfate and calcium sulfate will be removed from the process as part of the liquid concentrate. Finally, salts of sodium sulfite / sodium sulfate and calcium sulfate can be removed at chemical waste treatment plants, or further converted to a stream with a high solids content (for example, up to 100%), which can be placed in special chambers in a landfill to prevent reverse conversion sulfite / sulfates to a gas from organic waste, such as H ₂ S. Since the residual volume formed from landfill filtrate is usually a highly diluted waste water stream, usually only 3% of the original the total volume of wastewater even with added sulfite / sulfate salts, the costs of transportation and destruction at chemical waste processing plants outside the work site, or the costs of building and operating special chambers in a landfill to contain 100% solids in them, should be cost-effective , especially when compared with the costs of cleaning flue gas from emissions or removal of hydrogen sulfide before combustion without using the waste heat of the combustion process as the main source of energy A sewage treatment (e.g., filtrate).

This dual-purpose use for a wastewater treatment system provides tremendous benefits to landfill owners who find that emissions from flare plants or power plants using gas from organic waste as fuel exceed the established limits for SOx emissions. Converting a concentrator to work in a combined concentration / gas flushing mode only involves adding a metering system (for example, a pump connected to a concentrator controller) and a supply tank of the selected alkaline reagent used for gas flushing. Also, working changes to control the addition of the SOx removal step to the concentration method will not significantly increase the complexity of simple analytical tests that can be used to control both the levels of hydrogen sulfide in the gas from organic waste and the amount of sulfate in the concentrate produced during the implementation of the method.

As can be seen in FIGS. 3 and 10, the concentrating unit 120 may include an inlet 187 for caustic (or alkaline) material connected to a feed of caustic (or alkaline) material 193 (eg, sodium hydroxide or lime) using a feed line 189. Pump 191 may pressurize the caustic or alkaline material supply line 189 from the caustic or alkaline material supply tank 193 so that caustic or alkaline material is injected into the concentrating unit 120 (for example, through a section with Ilem venturi 162) to mix with the exhaust gas flare unit 130 or generator. In other implementations, the caustic or alkaline material may be mixed with the filtrate in the supply line of the filtrate 186 before being fed to the concentrating unit 120. Regardless of the method, after feeding the caustic or alkaline material to the concentrating unit 120, this material is quickly mixed with the exhaust gas in the concentrating unit 120 together with the filtrate as described above. After mixing, the caustic or alkaline material reacts with sulfur oxides, converting sulfur oxides to sodium sulfate and sodium sulfite or calcium sulfate, as described above. After conversion, sodium sulfate, sodium sulfite and / or calcium sulfate immediately go into the liquid phase, where they either remain in the dissolved state or precipitate from the gas-liquid mixture in the concentrating unit 120. Thus, sulfur, which was originally in the form of H ₂ S in the gas from organic waste, passes into the liquid phase and finally gets together with the concentrated filtrate into the sump 172 of the block of the mist eliminator 122 and can be removed together with the concentrated filtrate for further destruction. As shown in FIG. 9, a controller 302 can be operatively connected to a pump 191 to control the dispensing of caustic or alkaline material to the concentrating unit 120. The controller 302 can determine the correct caustic supply based on at least the mass flow of exhaust gas through the concentrating block 120 and the percentage of sulfur oxides in the exhaust gas. Thus, this concentrator can indeed be adapted to various components in the exhaust gas and / or various exhaust gas mass flow rates. As a result, this concentrator has the ability to simultaneously concentrate landfill filtrate and remove contaminants, such as sulfur oxides, from the exhaust gas from the flare of a landfill, reciprocating engine or turbine.

Ammonia removal

Ammonia is an air pollutant and causes granular formation in exhaust gases when released into the atmosphere. Since ammonia dissolves in water, it is usually found in wastewater (such as leachate) from landfills. Unlike gas from organic waste.

Known ammonia removal principles can be used in the context of the concentrator and purifier of the medium described herein. For example, wastewater containing ammonia can be treated with a substance (for example, caustic or alkali, such as sodium hydroxide or lime), which can increase the pH of the filtrate. The filtrate with a higher pH value can be fed to the aerator, where the ammonia contained in the wastewater will migrate to the exhaust air of the aerator. The exhaust air of the aerator can be connected to the combustion air and excess air used to operate the flare, piston engine or turbine, providing heat for the concentration method.

In a flare unit, reciprocating engine or turbine, ammonia from the combustion air can significantly reduce the amount of other pollutants, nitrogen oxides (NOx) that may be present in the combustion products. Such a reduction can be accomplished by implementing a method known as selective non-catalytic reduction of NOx emissions. When ammonia enters from the waste heat source into a hot gas concentrator, a reagent capable of converting ammonia to a stable salt (as when removing SOx with alkaline cleaning agents) can be introduced into the process. For example, sulfuric acid may be discharged into wastewater (e.g., filtrate) after being discharged from the aerator. This acid can be used to separate ammonia as ammonium sulfate (NH ₄ ) ₂ SO ₄ when it is in a concentrated liquid.

As shown in FIG. 17, an alternative embodiment of the concentrator used to remove ammonia from the landfill filtrate may include a caustic or alkali feed line 195 connected to the filtrate feed line 186. The combined caustic / filtrate stream can be fed through an integrated aerator 201 before being fed to the concentrator block 120. The aerator 201 can take out gaseous ammonia, which is released into the absorbing gas by means of pre-added acoustics or alkali. Selected gaseous ammonia can be delivered back to the flare unit 130 for gas from organic waste or to a reciprocating engine or turbine through an ammonia supply line 194. As described above, ammonia in the flare unit 130, piston engine or turbine can significantly reduce the amount of NOx. Independently, ammonia can be separated as a stable salt by adding the reagent from the reagent source 197 through the inlet of the reagent 199 in the concentrating unit 120. Thus, this concentrator can remove ammonia from the filtrate stream, converting ammonia into a by-product that is easily removed.

One aspect of the method for removing sulfur from gas from organic waste described in this document involves combining heated gas and a pressure wastewater stream to form a mixture, lowering the static pressure of the mixture to vaporize a portion of the liquid from the mixture to form a partially evaporated mixture containing transported concentrated liquid and a liquid concentrate, contacting the partially evaporated mixture with an alkaline material to reduce the content of sulfur oxides in the partially evaporated mixture, and removing part of the transferred end and liquid-centered reduced amount of sulfur oxides with the partially vaporized mixture for gas-free liquid.

Another aspect of the method for removing sulfur from gas from organic waste described in this document includes recycling and combining a liquid wastewater stream with a liquid concentrate.

Another aspect of the method for removing sulfur from a gas from organic waste described in this document includes removing a portion of the transferred concentrated liquid and a reduced amount of sulfur oxides from the partially evaporated mixture and passing the partially evaporated mixture through the cross-flow gas scrubber to remove part of the transferred concentrated liquid and the reduced amount of oxides sulfur with a partially evaporated mixture.

In another aspect of the method for removing sulfur from gas from organic waste described herein, a partially vaporized mixture has a temperature of from about 150 ° F to about 190 ° F (from about 66 ° C to about 88 ° C).

Another aspect of the method for removing sulfur from gas from organic waste, described in this document, includes the formation of exhaust gas during combustion of fuel.

Another aspect of the method for removing sulfur from gas from organic waste described in this document includes the selection of fuels from the group consisting of gas from organic waste, natural gas, propane, and combinations thereof.

Another aspect of the method for removing sulfur from gas from organic waste described in this document involves the combustion of gas from organic waste.

Another aspect of the method for removing sulfur from gas from organic waste described in this document involves the combustion of natural gas.

In another aspect of the method for removing sulfur from gas from organic waste described herein, the heated gas has a temperature of from about 900 ° F to about 1200 ° F (from about 482 ° C to about 649 ° C).

In another aspect of the method for removing sulfur from gas from organic waste described in this document, wastewater contains from about 1 wt.% To about 5 wt.% Solids based on the total weight of the filtrate.

In yet another aspect of the method for removing sulfur from gas from organic waste described herein, a liquid concentrate is likely to contain at least about 10 wt.% Solids based on the total mass of the concentrate, more likely a liquid concentrate contains at least about 20 wt.% Solids of the total weight of the concentrate, even more likely a liquid concentrate contains at least about 30 wt.% Solids of the total weight of the concentrate, and even more likely the liquid concentrate contains, at the edge at least about 50 wt.% solids of the total mass of the concentrate.

In yet another aspect of the method for removing sulfur from gas from organic waste described herein, a partially vaporized mixture contains from about 5 wt.% To about 20 wt.% Liquid, based on the total mass of the partially evaporated mixture, and more likely the partially evaporated mixture contains from from about 10 wt.% to about 15 wt.% liquid of the total weight of the partially evaporated mixture.

Another aspect of the method for removing sulfur from gas from organic waste described in this document involves the combustion of natural gas coming directly from the wellhead of natural gas.

Another aspect of the method for removing sulfur from gas from organic waste described in this document includes the selection of wastewater from the group consisting of filtrate, return water, produced water, and a combination thereof.

Another aspect of the method for removing sulfur from gas from organic waste described in this document includes the selection of alkaline material from the group consisting of sodium hydroxide, calcium carbonate, and mixtures thereof.

Another aspect of the method for removing sulfur from gas from organic waste, described in this document, involves combining heated gas and a liquid stream of wastewater containing alkaline material under pressure to form a mixture of them and to reduce the content of sulfur oxides, reducing the static pressure of the mixture to evaporate part liquid from the mixture to obtain a partially evaporated mixture containing a portable concentrated liquid and a liquid concentrate, and removing part of the portable concentrated liquid and reduced t he sulfur oxides from the mixture is partially evaporated to obtain a gas containing no liquid.

An aspect of the method for removing ammonia from the landfill filtrate described in this document includes combining an agent to increase the pH value with a liquid wastewater stream to form a wastewater stream with a higher pH value, contacting the air stream with a liquid pH wastewater stream under conditions sufficient to remove ammonia from the wastewater to produce an exhaust stream of air enriched with ammonia, wastewater with a high pH and a small amount of ammonia, combining heated gas with waste water with a high pH value and a small amount of ammonia, under pressure to form a mixture, reducing the static pressure of the mixture to evaporate part of the liquid from the mixture to obtain a partially evaporated mixture containing portable concentrated liquid and liquid concentrate, and removing part of the transferred concentrated liquid and reduced the amount of sulfur oxides from the partially evaporated mixture to obtain a gas without liquid content.

Another aspect of the method for removing ammonia from the landfill filtrate described herein involves combining an exhaust stream of air enriched with ammonia with a stream of air for combustion, and burning fuel in the presence of a combined stream of air to produce exhaust gas containing heated gas.

Another aspect of the method for removing ammonia from the landfill filtrate described in this document involves the selection of caustic as a material to increase the pH.

Another aspect of the method for removing ammonia from the landfill filtrate described herein involves the selection of sodium hydroxide and lime as caustic material.

Another aspect of the method for concentrating wastewater in accordance with the disclosure of this invention includes combining heated gas and liquid wastewater within an airtight portion of a channel to form a mixture that flows through the airtight channel under the influence of a vacuum created by an exhaust fan located after the airtight channel flowing mixture through a channel section with a limited cross-sectional area compared to the cross-sectional area where the mixture is created, thereby increasing the flow velocity and creating turbulence leading to the appearance of transverse forces between the continuous gas phase and the surfaces of the bounded channel opening in contact with the discrete liquid phase, which breaks up the droplets and other geometric shapes of the flowing liquid into very small drops, thereby creating an extended boundary surface between the flowing gas and liquid wastewater, which provides a quick approach to the temperature of adiabatic saturation of the liquid-gas mixture due to the rapid transfer of heat and m ssy from gas to liquid and liquid to gas, respectively, to produce partially vaporized mixture comprising tolerable concentrated liquid and liquid concentrate, and removing a portion of the concentrated liquid transferred from the evaporated mixture to obtain a gas containing no water.

Although certain of the presented embodiments and details have been shown to illustrate the invention, one skilled in the relevant art will understand that various changes to the methods and devices disclosed in this document can be made without departing from the scope of the invention.

Claims (30)

1. A method of concentrating wastewater with a heated gas containing sulfur oxides (SOx) and reducing the content of SOx therein, including:
but. combining heated gas and a liquid wastewater stream under pressure to form a mixture;
b. reducing the static pressure of the mixture to evaporate part of the liquid from the mixture to obtain a partially evaporated mixture containing a portable concentrated liquid and a liquid concentrate;
at. contacting the alkaline material with the partially evaporated mixture to reduce the content of sulfur oxides in the partially evaporated mixture; and
d. removing part of the concentrated concentrated liquid and the reduced amount of sulfur oxides from the partially evaporated mixture to produce a gas without liquid content. 2. The method according to claim 1, characterized in that it further includes recycling and combining the liquid concentrate with the liquid wastewater stream. 3. The method according to claim 1, characterized in that the removal of a part of the concentrated concentrated liquid and a reduced amount of sulfur oxides from the partially evaporated mixture includes the passage of the partially evaporated mixture through a cross-flow gas washing apparatus to remove part of the transferred concentrated liquid and the reduced amount of sulfur oxides from the partially evaporated mixture . 4. The method according to claim 1, characterized in that the partially evaporated mixture has a temperature of from about 66 ° C to about 88 ° C. 5. The method according to claim 1, characterized in that the heated gas contains exhaust gas generated during the combustion of fuel. 6. The method according to claim 5, characterized in that the fuel is selected from the group comprising gas from organic waste, natural gas, propane, and combinations thereof. 7. The method according to claim 6, characterized in that the fuel is a gas from organic waste. 8. The method according to claim 6, characterized in that the fuel is natural gas. 9. The method according to claim 1, characterized in that the heated gas has a temperature of from about 482 ° C to about 649 ° C. 10. The method according to claim 1, characterized in that the wastewater is selected from the group consisting of filtrate, return water, produced water, and combinations thereof. 11. The method according to claim 10, characterized in that the wastewater is a filtrate. 12. The method according to claim 1, characterized in that the wastewater contains from about 1 wt.% To about 5 wt.% Solids based on the total weight of the filtrate. 13. The method according to p. 12, characterized in that the liquid concentrate contains at least about 10 wt.% Solids from the total mass of the concentrate. 14. The method according to item 13, wherein the liquid concentrate contains at least about 20 wt.% Solids from the total mass of the concentrate. 15. The method according to 14, characterized in that the liquid concentrate contains at least about 30 wt.% Solids from the total mass of the concentrate. 16. The method according to clause 15, wherein the liquid concentrate contains at least about 50 wt.% Solids from the total mass of the concentrate. 17. The method according to claim 1, characterized in that the partially evaporated mixture in step b. contains from about 5 wt.% to about 20 wt.% liquid of the total weight of the partially evaporated mixture. 18. The method according to 17, characterized in that the partially evaporated mixture in step b. contains from about 10 wt.% to about 15 wt.% liquid of the total weight of the partially evaporated mixture. 19. The method according to claim 1, characterized in that the alkaline material is selected from the group comprising sodium hydroxide, calcium carbonate, and mixtures thereof. 20. The method according to claim 19, characterized in that the alkaline material further comprises a sodium hydroxide solution. 21. The method according to claim 19, characterized in that the alkaline material contains a suspension of calcium carbonate. 22. A method of concentrating wastewater with a heated gas containing sulfur oxides (SOx) and reducing the content of SO _x therein, including:
but. combining heated gas and a liquid wastewater stream containing alkaline material under pressure to form a mixture and reduce the content of sulfur oxides;
b. reducing the static pressure of the mixture to evaporate part of the liquid from the mixture to obtain a partially evaporated mixture containing a portable concentrated liquid and a liquid concentrate; and
at. removing part of the concentrated concentrated liquid and a reduced amount of sulfur oxides from the partially evaporated mixture to obtain a gas without liquid content. 23. A method of concentrating wastewater with a heated gas containing sulfur oxides (SOx) and reducing the content of SOx therein, including:
but. a combination of heated gas and liquid wastewater flow under pressure;
b. passing a combined stream of heated gas and a liquid wastewater stream through a mixing channel of a concentrator to form a gas-liquid mixture having a liquid concentration of from about 5 wt.% to about 20 wt.% of the total mixture, a mixing channel having a narrowed portion in which the gas-liquid stream within the mixing channel is accelerated when passing from the inlet to the outlet of the channel;
at. contact of the alkaline material with the gas-liquid mixture to reduce the content of sulfur oxides of the gas-liquid mixture;
d. separating part of the liquid from the gas-liquid mixture to obtain a gas mixture with portable liquid drops, wherein the liquid and liquid drops contain sulfur oxides;
e. removing droplets of liquid carried by the gas mixture obtained in step g to obtain concentrated liquid and gas, mostly free of liquid and SOx. 24. The method according to item 23, wherein the method includes recycling and combining with a liquid wastewater stream in step a. concentrated liquid obtained in step e. 25. A method of removing ammonia from wastewater and concentrating wastewater with a heated gas, including:
but. combining a pH increasing material with a liquid wastewater stream to form a wastewater stream with a higher pH value;
b. contact with the wastewater stream with a high pH value of the air stream under conditions sufficient to remove ammonia from the wastewater to obtain an exhaust stream of air enriched with ammonia, wastewater with a high pH value and a small amount of ammonia;
at. combining heated gas and wastewater with a high pH and a small amount of ammonia under pressure to form a mixture;
d. reducing the static pressure of the mixture to evaporate part of the liquid from the mixture to obtain a partially evaporated mixture containing a portable concentrated liquid and a liquid concentrate; and
d. removing part of the transferred concentrated liquid from the partially evaporated mixture to obtain a gas without liquid content. 26. The method according A.25, characterized in that it further includes combining the exhaust stream of air enriched with ammonia obtained in step b., With an air stream for combustion, and combustion of fuel in the presence of a combined air stream to form an exhaust gas containing heated gas used in step c. 27. The method according A.25, characterized in that the material that increases the pH value is caustic. 28. The method according to item 27, wherein the caustic material is calcium hydroxide or lime. 29. The method according to claim 8, characterized in that the natural gas is not cleaned and is supplied directly from the wellhead. 30. The method according to claim 8, characterized in that the natural gas is purified.

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