UA107800C2 - A compact and portable liquid concentrator of wastewater and gas washing unit to remove contaminants - Google Patents

Abstract

The compact mobile fluid concentrator comprises a gas inlet, a gas outlet and a flow channel, a connecting gas inlet and a gas outlet, and the flow channel contains a narrowed portion that increases the rate of gas flow through the flow channel. Through the inlet pipe, the liquid is injected into the gas stream in front of the narrowed area so that the gas-liquid mixture is completely mixed in the flow channel, causing partial evaporation of the liquid. The fog pickup or gas washer in the narrowed area removes the droplets of liquid carried away by the gas stream and returns the collected liquid to the liquid inlet through the recirculation circuit. The fresh concentration fluid is also fed to a recirculation circuit at a speed large enough to compensate for the amount of evaporated liquid in the flow channel.

Description

of suspended solids brought by wastewater and solids precipitated from the process liquid. 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 be carried out before having to stop work for the next cleaning. This negative effect imposes a limit on the amount of wastewater that can be effectively heated, especially if the wastewater contains scale-forming liquids. Therefore, methods operating on the principle of indirect heat transfer are generally unsuitable for concentrating most wastewater and ensuring 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 special type of direct heat transfer concentrator in which a bubbling heat exchange method is implemented in which gaseous combustion products are generated and fed through an inlet pipe to a dispersing device immersed into a technological liquid. The dispersing device includes a plurality of spaced gas outlet tubes radially diverging from the inlet tube, each gas outlet tube having small openings spaced apart at various locations along the surface of the gas outlet tube to allow gaseous products to be discharged. combustion in the form of small bubbles as uniformly as practicable over the entire cross-section of the liquid subject to heating in the working vessel. According to modern ideas about known devices of this type, this concentrator provides the necessary tight contact between liquid and hot gas on a large surface of the phase interface. The peculiarity of this process is that both heat exchange and mass exchange take place under dynamic conditions on the constantly renewed interphase surface, which is formed as a result of bubbling of the gas phase through the process liquid, 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 holes in the gas discharge tubes, which are used to distribute hot gases by volume of process liquid in the concentrator according to US patent Mo 5,342,482, become clogged with solids that settle from the scale-forming liquids. As a result, the inlet pipe, through which hot gases are fed into the process liquid, is covered with a crust of solid sediment.

Because of the need to pass a large volume of gas through a continuous flow of the liquid phase, the concentrator vessel proposed in US Pat. No. 5,342,482 must typically 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 effect of changing concentrations of the hot technological environment during the operation of the system. In systems designed for the treatment of a wide variety of wastewater, the structural materials of the wetted surface require special design solutions regarding corrosion resistance and temperature resistance, which must take into account the cost of the equipment and the costs of its maintenance and replacement after a certain period of time. Generally speaking, increased life and reduced wetted surface maintenance/replacement costs are achieved by choosing either high-quality metal alloys or certain structural plastics, similar to those used to manufacture fiberglass vessels. But the usual methods of concentration, using indirect or direct heating systems, also require devices for supplying hot coolants, 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, vessels and fittings made from them are very expensive. On the other hand, although structural plastics can be used for the manufacture of the entire vessel as a whole or as a coating on a wetted surface, 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 the US patent Mo 5,342,482, 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, all of these systems require a heat source in order for concentration or evaporation to take place. Many systems have been developed that use heat from various sources, such as heat from an engine, a combustion chamber, or a gas compressor, as a heat source for wastewater treatment. A description of one of these systems is given in US patent Mo 7.214.290. In this system, heat is generated by burning gas released from organic waste and used in a submerged gas evaporator to treat wastewater at the landfill. US Patent No. 7,416,172 describes a submersible gas evaporator in which waste heat can be supplied to the inlet of the gas evaporator for use in concentrating or vaporizing 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 the landfill will be powered by electric generators that use one or more internal combustion engines that use gas produced from organic waste as fuel. The exhaust gases of these engines, which are usually released through the muffler and exhaust pipe into the atmosphere on the roof of the building in which the generators are located, are a source of waste heat. But in order to collect and use this waste heat, it is necessary to connect a significant amount of expensive pipes and pipes to the exhaust pipe and supply the waste heat to the place where the treatment system is located, which is usually located at the zero mark away from the building in which 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 the high temperatures that the exhaust gases have in the exhaust pipe (for example, 510 "C) and they have to be insulated so that the exhaust gases were not cured during transportation. The materials used to insulate them are prone to failure due to a number of factors, such as brittleness, susceptibility to erosion after a certain period of time, and sensitivity to cyclic temperature fluctuations, which further complicates the construction. Insulation also increases the weight of the pipes , pipelines and regulatory devices, which leads to an increase in the price of support structures.

The essence of the invention

The compact liquid concentrator proposed here can easily be connected to a waste heat source, such as an organic waste gas flare or an internal combustion engine exhaust pipe, and use this waste heat to perform direct heat transfer concentration without the use of large expensive vessels and many expensive temperature-resistant materials. The compact liquid concentrator includes a gas inlet, a gas outlet, and a mixing or flow channel connecting the gas inlet to the gas outlet, wherein the flow channel has a narrowed section in which the gas flow rate through the flow channel increases. Through the nozzle for the supply of liquid, located between the gas inlet nozzle and the narrowed section of the flow channel, a liquid is injected into the gas flow at a point before the narrowed section so that the gas-liquid mixture is completely mixed in the flow channel, leading to evaporation or concentration of a portion of the liquid. In the fog trap or gas cleaner, located behind the narrowed section and connected to the gas outlet nozzle, liquid droplets carried by the gas flow are separated, and the collected liquid is returned to the nozzle for feeding it through the recirculation circuit. Fresh liquid entering the concentration is also introduced into the recirculation circuit at a rate sufficient to compensate for the total decrease in the amount of liquid due to its evaporation in the flow channel and due to the removal of the concentrated liquid.

The proposed compact liquid concentrator is characterized by a number of features that ensure cost-effective concentration of wastewater, which differ significantly from each other in terms of their parameters. The concentrator is distinguished by its corrosion resistance in relation to wastewaters that differ significantly from each other in terms of their parameters, has a moderate manufacturing cost and acceptable operating costs, is capable of continuous operation at a high degree of concentration, and efficiently uses heat energy directly from a variety of sources. In addition, the concentrator is compact enough to be moved during transport to locations where wastewater has been generated by uncontrolled events and installed directly near waste heat sources. Thus, the proposed concentrator is a cost-effective, reliable device characterized by a considerable service life, which in a continuous mode concentrates wastewaters that differ significantly from each other in terms of their parameters, and thus allows doing without conventional heat exchangers with a solid heat exchange surface used in ordinary systems with indirect heat transfer, which are subject to clogging and overgrown with a crust of scale.

A brief description of the drawings

In fig. 1 shows a general diagram of a compact liquid concentrator.

In fig. 2 shows an embodiment of the liquid concentrator, the diagram of which is shown in fig. 1 mounted on a liquid sump or sled to facilitate its transport on a truck.

In fig. C shows a perspective view of a compact liquid concentrator, which implements the method of concentration, the scheme of which is shown in Fig. 1, connected to a source of waste heat, which is a torch for burning gas that is released from organic waste.

In fig. 4 shows a perspective view of the heat transfer unit of the compact liquid concentrator shown in Fig. 3.

In fig. 5 is a perspective view of the evaporation/concentration unit of the compact liquid concentrator shown in FIG. 3.

In fig. 6 is a perspective view of the easy-to-open inspection hatches on the compact fluid concentrator unit shown in FIG. 3.

In fig. 7 is an open perspective view of one of the easy-to-open inspection hatches shown in FIG. 6.

In fig. 8 is a perspective view of the easy-to-open locking mechanism used on the manholes shown in FIG. 6 and 7.

In fig. 9 is a schematic representation of a control system that can be used to control the various units in the compact fluid concentrator shown in FIG. 3.

In fig. 10 shows an image of the compact liquid concentrator shown in fig. 3, which is connected to the exhaust pipe of the combustion engine as a source of waste heat.

Fig. 11 shows a schematic representation of another embodiment of a compact liquid concentrator.

In fig. 12 is a top view of the compact liquid concentrator shown in fig. 11.

In fig. 13 shows a schematic representation of a third embodiment of a compact liquid concentrator, which is a distributed liquid concentrator.

In fig. 14 shows an enlarged cross-section of the fluid concentration unit of the distributed fluid concentrator shown in FIG. 13.

In fig. 15 is a top view of the liquid concentration block shown in fig. 14.

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

In fig. 17 is a perspective view of an alternative embodiment of a compact liquid concentrator that provides the method of concentration depicted in FIG. 1 and is configured to remove ammonia from landfill leachates.

Detailed description of the invention

In fig. 1 shows the general scheme of the liquid concentrator 10, which contains a gas outlet nozzle 20, a gas outlet hole 22 and a flow channel 24 connecting the gas outlet nozzle 20 with a gas outlet hole 22. The flow channel 24 has a narrowed section 26, in which the speed of gas flow along the flow channel increases channel 24 and at this point or near it in the flow channel 24 a turbulent flow occurs. The narrowed section 26 in this embodiment may be a venturi device. Through the liquid supply nozzle 30, the liquid to be concentrated (by evaporation) is injected into the liquid concentration chamber in the flow channel 24 at a point before the narrowed section 26, and the injected liquid is mixed with the gas flow in the flow channel 24. The liquid supply nozzle 30 can contain one or more variable nozzles 31 designed to inject liquid into the flow channel 24. The inlet nozzle 30, regardless of whether it contains a nozzle 31 or not, can supply liquid into the flow channel 24 at any angle, in particular perpendicular and parallel to the gas flow . A partition 33 can also be located near the nozzle for supplying liquid 30 in such a position that the liquid coming from the nozzle 30 is reflected from it into the flow channel in the form of small drops.

When the gas-liquid flow flows through the narrowed section 26 according to the Venturi effect, the speed increases and a turbulent flow occurs, which completely mixes the gas and liquid in the flow channel 24 near the nozzle 30 and behind it. Acceleration when flowing through the narrowed area 26 creates transverse forces acting between the gas flow and liquid drops, as well as between the liquid drops and the walls of the narrowed area 26, which leads to the formation of very small liquid drops drawn into the gas, thus increasing the surface area of the boundary between liquid droplets and gas and contributing to the rapid transfer of mass and heat between gas and liquid droplets. The liquid exits the narrowed area 26 in the form of very small drops of liquid regardless of the geometric shape of the liquid supplied to the narrowed area 26 (for example, the liquid may enter the narrowed area 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 flow. When the gas-liquid mixture flows through the narrowed section 26, the direction and/or speed of the gas-liquid mixture flow can be changed with the help of adjustable flow restrictors, such as the venturi plate 32, which is mainly used to create a large pressure difference in the flow channel 24 before and after the plate Venturi 32. Plate position

The venturi 32 can be adjusted to change the size and/or shape of the constricted section 26, and it can be made of a corrosion-resistant material, particularly a high quality alloy such as "hastelloy", "iInconel" or "monel".

From the narrowed section 26, the gas-liquid mixture enters the mist catcher 34 (also called a gas cleaner or a droplet catcher), connected to the gas outlet 22. The mist catcher 34 removes the liquid droplets carried by it from the gas flow. The fog trap 34 contains a gas channel. The separated liquid accumulates in the liquid collector or liquid settler 36 in this gas passage, and the liquid settler 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 this vessel, designed to feed the liquid through the recirculation circuit 42 back to the liquid supply nozzle 30 and/or the flow channel 24. Thus, the volume of the liquid can be reduced by evaporation to required degree of concentration. Fresh or new liquid directed to concentration is supplied to the recirculation circuit 42 through the nozzle for supplying liquid 44.

Instead, new liquid can be injected into the direct flow channel 24 in front of the venturi plate 32. The rate of fresh liquid supply to the recirculation circuit 42 can be equal to the sum of the rate of evaporation of the liquid when the gas-liquid mixture passes through the flow channel 24 and the rate of liquid withdrawal through the nozzle for the selection of concentrated liquid 46, located on or near the separated liquid storage vessel 40. The ratio of volume of circulating liquid to volume of fresh liquid can generally be in the range of 1:1 to 100:1, but is usually in the range of 5:11 to 25 :11. For example, if in the recirculation circuit 42 the fluid circulates at a rate of about 38 L/min, then fresh or new fluid can be supplied at a rate of about 3.8 L/min. (ie relative to 10:1). It will be possible to withdraw part of the liquid through the nozzle for the withdrawal of concentrated liquid 46 after the liquid in the recirculation circuit 42 reaches the required level of concentration. The recirculation circuit 42 acts as a buffer or shock absorber in the evaporation method, ensuring that there is a sufficient amount of 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 trap 34, the gas flow enters the exhaust fan 50, which sucks the gas through the flow channel 24 and the gas passage channel of the mist trap, creating vacuum. Of course, the concentrator 10 could also work at increased pressure created by a gas blower (not shown in the figure), placed in front of the nozzle for supplying liquid 30.

Finally, the gas is released into the atmosphere through the gas outlet 22 or sent for further processing.

The concentrator 10 may contain a pretreatment system 52 designed to process the concentrated liquid, which may be wastewater. For example, as a pretreatment system 52, an air deodorizer designed to remove substances capable of creating an unpleasant odor or controlled as air pollutants can be used. In this case, the air deodorizer can be an air deodorizer of the usual type, or it can be another concentrator of the type offered here, which can be connected in series as an air deodorizer. In the pre-treatment system 52, the concentrated liquid may be heated in any suitable manner if necessary. In addition, the gas and/or wastewater circulating through the concentrator 10 may be preheated in the heater 54. Preheating may be used to increase the rate of evaporation, and subsequently, 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 their mixtures, fossil fuels or by using waste heat. In addition, preheating of gas and/or wastewater can be done by using the waste heat generated in the exhaust pipe or in the flare to burn the gas that is released from the organic waste. Waste heat from an engine, such as an internal combustion engine, can also be used to preheat 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 a gas well in a raw state or immediately after the completion of the gas well equipment until the stabilization of the gas flow or after the stabilization of the gas flow in a more stable mode of the natural gas well. Additionally, natural gas can be cleaned before being burned in a flare. In addition, the gas flow coming from the gas outlet 22 of the concentrator 10 can be fed to a flare unit or some other device for further treatment 56, designed to treat the gas before it is released into the atmosphere.

The liquid concentrator 10 provided herein can be used to concentrate a variety of wastewaters, such as industrial wastewater, wastewater generated from natural disasters (floods, hurricanes), spent caustic or leachate such as landfill leachate, return water from completed natural wells gas, reservoir water, which comes during the operation of natural gas wells, etc. Liquid concentrator 10 is easy to operate, energy-efficient, reliable and cost-effective. The utility of this fluid concentrator is further enhanced by the ability to mount the fluid concentrator 10 on a trailer or mobile sled to successfully treat wastewater generated from accidents and natural disasters, or be used for routine wastewater treatment of spatially dispersed or remote objects.

The proposed liquid concentrator 10 is characterized by all the necessary parameters and provides significant advantages over conventional liquid concentrators, especially when it is necessary to process a wide variety of wastewater.

In addition, the concentrator 10 can be made mainly of materials characterized by high corrosion resistance of low-cost materials, such as fiberglass and/or other structural plastics. This possibility is partly due to the fact that the proposed concentrator is designed to work at a minimum differential pressure. For example, the differential pressure should generally have a value in the range from 254 to 762 cm of water column. And since in the zone of contact of gas with liquid when the concentration method is reduced, strong turbulence occurs inside a limited (compact) passage in the area with a Venturi profile or immediately behind it, the whole design as a whole is very compact compared to conventional concentrators, in which contact of gas with liquid flows in a large process vessel. As a result, the amount of high-quality metal alloys required to manufacture the hub 10 is quite small. And since the size of parts made from 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 reduced even further by designing some or all of these worn parts with less quality alloys and by periodically replacing them. If necessary, these lower quality alloys (e.g. carbon steel) can be coated with a corrosion-resistant and/or erosion-resistant lining material such as structural plastics, including elastomeric polymers, to extend the life of such parts. Similarly, the pump 40 can be coated with a corrosion-resistant and/or erosion-resistant lining material to increase the life of the pump 40 and thus provide further reductions in maintenance and parts replacement costs.

It is clear that the liquid concentrator 10 provides direct contact of the liquid to be concentrated with the hot gas, creating heat exchange and mass transfer between the hot gas and the liquid, for example, sewage to be concentrated, in a powerful turbulent mode. In addition, the concentrator 10 creates a very compact zone of gas-liquid contact, making it minimal in size compared to known concentrators. Direct contact heat transfer improves energy efficiency and eliminates the need for solid surface heat exchangers used in conventional indirect heat transfer concentrators. In addition, the compact zone of gas-liquid contact makes bulky process vessels used in conventional concentrators of indirect or direct heat transfer unnecessary. These features make it possible to manufacture the concentrator 10 with a small mass compared to conventional concentrators using a comparatively cheap manufacturing technology.

Both of these factors increase its portability and profitability. Thus, the liquid concentrator 10 is more compact and lighter than conventional concentrators, which makes it ideally suited as a mobile installation. In addition, the liquid concentrator 10 is less prone to clogging and clogging due to heat exchange by direct contact and the absence of solid heat exchange surfaces. Due to heat transfer by direct contact, the liquid concentrator 10 can also be used to treat liquids containing a significant amount of suspended matter. As a result, it is possible to achieve a high degree of concentration without frequent cleaning of the concentrator 10.

In particular, in liquid concentrators in which indirect heat transfer is used, heat exchangers are prone to clogging and subject to accelerated corrosion at normal operating temperatures of the coolant circulating in them (steam or other hot liquid medium). Each of these factors imposes significant limitations on the lifetime and/or cost of construction of conventional indirect heat transfer concentrators, and on how long they can operate before they need to be shut down and the heat exchangers cleaned or repaired. As a result of the rejection of bulky process 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 liquid, the relatively small volume of liquid in the system, and the low relative humidity of the gas before mixing 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 in the range from 66 "C to 102 "C (ie, the hub is a "low-inertia" hub).

In addition, the concentrator 10 is designed to operate under vacuum, which greatly facilitates the use of a variety of fuels or waste heat sources as an energy source for evaporation. In fact, due to the flow design of these systems for heating and supplying gas to the concentrator 10, both supercharged and non-supercharged burners can be used. Simplicity of design and reliability of the concentrator 10 are provided by the minimum number of moving parts and the minimum need for spare parts. In general, a concentrator requires only two pumps and one exhaust fan if it is designed to operate on waste heat, such as exhaust gases from engines (such as generator engines or automobiles), flue gases from industrial pipes, gas compressor systems, and flares used , for example, for burning gas released from organic waste. These features provide significant advantages in that they favorably affect the operational flexibility and costs of purchasing, operating and maintaining the hub 10.

The hub 10 can operate in a startup state or a steady state. In the start-up state, the mist collector sump 34 and recirculation circuit 42 can be filled with fresh wastewater.

During the initial treatment, the fresh wastewater supplied to the liquid inlet 30 is at least partially vaporized in the constricted area 24 and settles in the mist trap sump 34 in a more concentrated form than the fresh wastewater. After a certain time, the waste water reaches the required concentration level in the fog trap 34 and the recirculation circuit 42. From now on, the concentrator 10 can operate in a continuous mode, in which the amount of solid particles removed to the nozzle for the collection of concentrated liquid 46 is equal to the amount of solid particles that arrived in the fresh wastewater through the nozzle for the supply of liquid 30. In the same way, the amount of water that evaporated in concentrator 10, is replaced by the same 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. As a result, the high efficiency of the concentrator 10 is achieved.

In fig. 2 is a side view of a liquid concentrator 10 mounted on a mobile bed 60, such as a liquid sump, trailer, or sled. The mobile bed is sized and shaped to be easily loaded onto a vehicle or hitched to a vehicle 62, such as a tractor-trailer. Likewise, a hub mounted on such a bed can easily be loaded onto a train, ship, or plane (not shown) for rapid delivery to remote locations. The fluid concentrator 10 can operate as a fully autonomous unit having its own burner and fuel supply system, or the fluid concentrator 10 can use an on-site burner and/or fuel or waste heat source. The fuel for the concentrator 10 can be renewable fuels, such as waste (for example, paper or wood shavings) and gas released 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 concentrator 10 installed on a trailer is capable of processing at least 380 m3 of wastewater per day, while large stationary units installed at landfills, wastewater treatment plants, or gas or oil fields are capable of processing hundreds of cubic meters. m of wastewater per day.

In fig. C shows a specific embodiment of a compact liquid concentrator 110 that operates using the principles described above with reference to FIG. 1, which is connected to a source of waste heat in the form of a flare unit for burning gas released from organic waste. Generally speaking, the compact liquid concentrator 110 shown in FIG. 3, intended for the concentration of wastewater, such as landfill leachate, using waste or waste heat generated in a flare unit from the combustion of organic waste gas, as specified in the standards of the US Environmental Protection Agency ( EPA) and/or more local regulatory bodies. As you know, most landfills have a flare unit used to burn off-gas from organic waste to remove methane and other gases from it before it is released into the atmosphere.

Usually, the gas at the outlet of the flare installation has a temperature in the range from 538 "C to 816 "C, but it can be heated up to 982 "C. The compact liquid concentrator 100, shown in Fig. 3, is equally effective in concentrating return water or formation water with natural gas wells and may use waste gas from a natural gas flare, or a propane flare located at or near the wellhead.In some applications, the natural gas feed to the natural gas flare may be directly from the natural gas well.

As shown in fig. 3, the compact liquid concentrator 110 is usually attached to the flare unit 115 and includes a heat transfer unit 117 (shown in an enlarged view in Fig. 4), a unit for pretreatment of air 119, a concentrating unit 120 (shown in an enlarged view in Fig. 5), a gas scrubber unit 122 and exhaust unit 124. An important feature is that the flare unit 115 contains a flare 130, in which the gas emitted from organic waste is burned in any known way, and a flare-cap unit 132. The flare-cap unit 132 contains a hinged a cap 134 (e.g., flare cap or exhaust cap) that covers the top of the flare 130 or other type of exhaust pipe (e.g., flue gas exhaust) when the flare cap 134 is in the closed position, or diverts a portion of the flare gas when the flare gas is partially covered, and which allows the flue gas produced in the flare 130 to escape to the atmosphere through the open end, which forms the primary ha outlet hole 143 when the torch cap 134 is in the open or partially open position. The torch cap unit 132 also includes a cap drive 135, which is a motor (eg, an electric motor, hydraulic motor, or pneumatic motor shown in FIG. 4) that moves the torch 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 about a pivot 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 attached to the flare cap 134 to turn the torch cap 134 around the pivot axis 136.

Flare cap assembly 132 may also include a counterweight 137 located on the opposite side of the pivot axis 136 of the flare cap 134 to counterbalance some of the weight of the flare cap 134 as it moves the flare cap 134 about the pivot axis 136.

The counterweight 137 allows the actuator 135 to be reduced in size or its power reduced enough that it can still rotate the flare cap 134 between an open position in which the top of the flare 130 (or primary gas outlet 143) is open to the atmosphere, and 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 may be made of a high temperature resistant material, such as stainless steel or carbon steel, and may be lined with a refractory material, such as alumina and/or zirconia, on the underside that directly contacts the hot flare gases. , when the torch cap 134 is in the closed position.

If necessary, the flare 130 may be provided with a transition device 138 that includes a primary gas outlet 143 and a secondary gas outlet 141 in front of the primary gas outlet 143. When the flare cap 130 is in the closed position, flue gases are discharged through the secondary gas outlet 141. Transition device 138 may have a fitting 139 that connects the torch 130 (or exhaust pipe) to the heat transfer unit 117 using a 90-degree elbow or bend. You can use other connecting devices. For example, the torch 130 and the heat transfer unit 117 can be connected at essentially any angle in the range from 0 to 180 degrees. In this case, the torch-cap unit 132 is installed on top of the transition device 138 near the primary gas outlet 143.

As shown in fig. With and 4, the heat transfer unit 117 includes a heat transfer pipe 140 that connects the inlet nozzle of the air pretreatment unit 119 with the torch 130, and more precisely, with the transition device 138 of the torch 130. The heat transfer pipe 140 between the torch 130 and the air pretreatment unit 119 lies at a certain height above the ground, resting on a stand in the form of a vertical beam or pillar. The heat transfer pipe 140 is connected to the fitting 139 or to the secondary gas outlet pipe 141 of the transition device 138, forming a channel between the transition device 138 and the device for carrying out a secondary process, such as liquid concentration. The support strut 142 is usually unnecessary because the heat transfer tube 140 is made of a metal such as carbon or stainless steel and can be lined with materials such as aluminum oxide and/or zirconium oxide so that it can withstand the temperature of the gas being supplied from the torch 130 to the air pretreatment unit 119. Thus, the heat transfer pipe 140 is usually a heavy piece of equipment.

However, the torch 130, on the one hand, and the air pretreatment unit 119 and the concentrator unit 120, on the other hand, are located directly next to each other, so the heat transfer pipe 140 should be relatively short, which will help reduce the cost of materials used in the concentrator 110, as well as the cost of the load-bearing structures that hold the heavy parts of the hub 110 above the ground. As shown in fig. 3, the heat transfer pipe 140 and the air pretreatment unit 119 form an O-shaped structure turned upside down.

The air pretreatment unit 119 includes a vertical pipe 150 and an atmospheric air inlet valve (not clearly shown in Fig. 3 and 4) located on top of the pipe 150. The atmospheric air inlet valve (also called an air valve) forms a passage between the heat transfer pipe 140 (or air pretreatment unit 119) and the atmosphere.

An atmospheric air inlet valve allows atmospheric air to enter through the wire screen 152 used for bird protection and to mix within the air pretreatment unit 119 with the hot gas from the flare 130. If necessary, the air pretreatment unit 119 may have a continuous an open window next to the air valve, which will always admit a certain amount of air into the air pretreatment unit 119, and this window allows to reduce the size of the required air valve and increase the safety of operation of the concentrator. A pressure booster (not shown) may be connected to the intake side of the atmospheric air valve if necessary to increase the passage of atmospheric air through the atmospheric air valve. When using a pressurizer, a bird screen 152 and a permanently open window (if used) can be attached to the inlet side of the pressurizer. Although 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 flare 130 to be cooled to a more acceptable temperature before it enters the concentrator unit 120. Air Pretreatment Unit 119 may partially rest on cross members 154 attached to support post 142. Cross members 154 stabilize air pretreatment unit 119, which is also typically made of heavy carbon or stainless steel or other metal and may be lined to improve energy efficiency and temperature resistance in this area of the concentrator 110. If necessary, the vertical pipe 150 can be extended to use it for flares of different heights, and thus make the liquid concentrator 110 suitable for many different flares or for flares of different heights. This principle is explained in more detail with reference to fig. 3. As shown in fig. 3, the standpipe 150 includes a first section 150A (shown in dashed lines) that fits inside the second section 1508 and thus allows the length (height) of the standpipe 150 to be adjusted.

Generally speaking, the air pretreatment unit 119 serves to mix the atmospheric air arriving through the atmospheric air intake valve below the wire screen

152, with the hot gas flowing from the flare 130 through the heat transfer pipe 140 to obtain gas having the required temperature at the inlet to the concentrator unit 120.

The concentrating unit 120 includes a guide section 156 with a reduced cross-section, the upper end of which is connected to the lower end of the vertical pipe 150, and the lower end is connected to the cooler 159 of the concentrating unit 120. The concentrating unit 120 also includes a first fluid inlet 160 through which new or untreated liquid directed to concentration, for example, as landfill leachate, is injected into the cooler 159. The nozzle 160 may contain, although this is not shown in fig. C, a large drop sprayer with a large cross-section nozzle for injecting raw liquid into the cooler 159. The liquid injected into the cooler 159 at this point in the system has not yet been concentrated, so it contains a large amount of water, and the sprayer has a large cross-section, so the sprayer nozzle is not contaminated and is not clogged with small particles contained in the liquid. It is clear that the cooler 159 is designed to rapidly reduce the temperature of the gas stream (for example, from 482 "C to 93 C) as a result of the strong vaporization of the liquid injected through the inlet nozzle 160. If necessary, it can be installed, although it is 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 adjust the position of the closing body of the atmospheric air inlet valve and thus to adjust the gas temperature in the inlet pipe of the concentrating unit 120.

As shown in fig. 5 and 5, the cooler 159 is connected to a fluid injection chamber attached to a narrowed section or section with a venturi profile 162, which has a narrower cross-section compared to the cooler 159 and which includes a venturi plate 163 (shown in dashed lines).

The venturi plate 163 creates a constricted passage in the venturi section 162, which results in the creation of a significant pressure drop between the inlet and outlet of the venturi section 162. This significant pressure drop creates a turbulent gas flow in the cooler 159 and at the top or inlet of the venturi section 162. venturi profile 162 and forces the gas to flow out of the venturi profile section 162 at a high speed, and all this leads to complete mixing of gas and liquid in the venturi profile section 162. The position of the venturi plate 163 can be adjusted with the manual control knob 165 (shown in Fig. 5 ), connected to the hinge axis of the plate 163, or with the help of an electric motor or a pneumatic cylinder (not shown in Fig. 5).

The recirculation pipe 166 covers from opposite sides the entrance to the section with the venturi profile 162 and serves to inject a partially concentrated (ie, circulating) liquid into the section with the venturi profile 162 in order to further concentrate it and/or prevent the formation of dry particles inside the concentration unit 120, through many liquid inlets located on one or more sides of the flow channel. Although in fig. 5 and 5, it is not obvious and not indicated that from each of the opposite branches of the tube 166 that partially enclose the venturi section 162, multiple tubes, for example three 1.77 cm diameter tubes, may branch off and penetrate through the walls into the venturi section 162 .Since the fluid entering the concentrator 110 at this point is a circulating fluid and is therefore either partially concentrated or has reached a certain equilibrium concentration and is more likely to clog the spray nozzles than the less concentrated fluid injected through the nozzle 160 , then this liquid should be injected directly from the tubes, without sprayers, to avoid clogging. However, if desired, a baffle in the form of a flat plate can be installed in front of each opening of the 1.77 cm tubes to cause the liquid entering the system at that point to break up on impact with the baffle into small droplets and disperse in the concentrator unit 120. Having this configuration , this recirculation system better distributes or sprays the recirculation liquid throughout the gas stream within the concentrator unit 120.

The mixture of hot gas and liquid flows in a turbulent mode through the venturi profile section 162. As mentioned above, the venturi profile section 162, which has a moving venturi plate 163 located across the concentrating unit 120, causes the flow to be turbulent and the liquid and gas are completely mixed, which contributes to the rapid evaporation of the liquid in the gas. Since the stirring action provided by the venturi section 162 provides a high degree of evaporation, the gas is substantially cooled by the concentrator unit 120 and exits the venturi section 162 into the submerged elbow 164 at a high velocity. In fact, the temperature of the gas-liquid mixture at this point can be about 71 °C.

As is common for submerged elbows, a spillway device (not shown) at the bottom of the submerged elbow 164 maintains a constant level of partially or fully concentrated recirculation fluid entering it. Drops of recirculation liquid, involved in the gas phase at the exit of the gas-liquid mixture from the section with a venturi profile 162, are brought at a high speed to the surface of the recirculation liquid, which is held in the lower part of the flooded elbow 164 by the vdenter force, which occurs when the gas-liquid mixture is forced to turn 90 degrees , to enter the gas scrubbing unit 122. A significant number of liquid droplets entrained in the gas phase, which contacts the surface of the recirculating liquid contained in the lower part of the flooded elbow 164,

is connected to the recirculation liquid, which leads to an increase in the volume of the recirculation liquid in the lower part of the flooded elbow 164 and ensuring the equality of the amount of recirculation liquid leaking from the overflow device and flowing under the action of gravity into the sump 172 in the lower part of the gas washing unit 122. Thus thus, as a result of the interaction of the gas-liquid flow with the liquid in the submerged elbow 164, liquid droplets are removed from the gas-liquid flow and the collision of suspended particles contained in the gas-liquid flow with the bottom of the submerged elbow 164 at high speed is avoided, and thus prevents erosion of the metal wall of the submerged elbow 164.

From the flooded elbow 164, the gas-liquid flow, which contains evaporated liquid, a certain number of liquid droplets and other particles, enters the gas washing unit 122, which in this case is a cross-flow gas washing apparatus. The gas scrubbing unit 122 contains various screens or filters that help remove entrained liquid from the gas-liquid stream and remove other particles that may be present in the gas-liquid stream. In one particular embodiment, the cross-flow gas scrubber 122 may include a front large-cell baffle 169 at the inlet, which is designed to remove liquid droplets of 50 μm to 100 μm in size.

Behind it, two replaceable pleated filters 170 are located across the stream flowing through the gas scrubber unit 122, and the filters 170 can gradually change in size or configuration to allow for the removal of progressively smaller droplets, such as 20-30 microns and less than 10 microns. Of course, you can use more or less filters or pleated filters.

As in conventional cross-flow scrubbers, the liquid captured by the filters 169 and 170 and the overflow chamber in the lower part of the flooded elbow 164 flows by gravity into a liquid reservoir or sump 172 located in the lower part of the gas scrubber unit 122. The liquid sump 172, which can accommodate, for example, 760 liters of liquid, collects the concentrated liquid containing dissolved and suspended solids removed from the gas-liquid stream and serves as a source of recirculating concentrated liquid that is fed back to the concentrating unit 120 for further processing and/or to prevent the formation of dry particles in concentration unit 120 as described above with reference to FIG. 1. In one embodiment, the liquid sump 172 may have a sloped M-shaped bottom 171 that has an M-shaped trough running from the rear side of the gas purge unit 122 (farthest from the submerged elbow 164) to the front side of the gas purge unit 122 (closest to flooded elbow 164), and the M-shaped chute 175 is inclined so that the bottom of the M-shaped chute 175 is lower at the end of the gas purge block 122 closest to the flooded elbow 164 than at the end of the gas purge block 122 remote from the flooded elbow 164. In other words, The M-shaped bottom 171 may slope toward the lowest point of this M-shaped bottom 171, which is near the toilet hatch 173 and/or the pump 182. In addition, the concentrated liquid from the liquid sump 172 may be supplied by a pump of the flushing circuit (not shown in the figures ) into an atomizer (not shown) inside the gas purge unit 122, and this atomizer is designed to spray liquid onto the M-shaped bottom. In addition, the concentrated liquid from the liquid sump 172 can be supplied by the pump of the washing circuit 177 (Fig. 9) to the sprayer 179 inside the cross-flow gas scrubbing unit 122, and this sprayer 179 is designed to spray the liquid on the M-shaped bottom 171. But the sprayer 179 can spray on the M-shaped bottom 171 and non-concentrated liquid or clean water. The sprayer 179 can periodically or continuously spray liquid onto the surface of the M-bottom 171 to wash away solids and prevent sediment from being deposited on the M-bottom 171 or on the toilet hatch 173 and/or the pump 182. Due to the presence of this

M-shaped inclined bottom 171 and washing circuit 177, the liquid that has accumulated in the liquid sump 172 is constantly mixed and renewed and thus keeps its consistency relatively unchanged and leaves the solids in a suspended state. If desired, the spray system 177 may be a separate circuit using a separate pump that is attached to, for example, the inlet side of the sump 172, or may use a pump 182 coupled to the concentrate liquid recirculation circuit described below to spray the concentrate liquid from the liquid sump 172 on M-shaped bottom 171.

As shown in fig. 3, the return line 180, as well as the pump 182 serve to return the liquid removed from the gas-liquid flow, from the sump 172 for the liquid back to the concentrator 120 and thus close the liquid recirculation circuit. Similarly, a pump 184 can be installed on the feed line 186 to supply new or untreated liquid, such as landfill leachate, through a nozzle 160 to a concentrator unit 120. Within the gas scrubber unit 122, one or more sprayers 185 can also be installed near the pleated filters 170 so that they could periodically spray clean water or a portion of the supplied wastewater onto the pleated filters 170 to wash them.

The concentrated liquid can also be removed from the liquid sump of the gas scrubbing unit 122 through the toilet hatch 173 and then subjected to further treatment or disposed of accordingly to the secondary recirculation circuit 181. In particular, the concentrated liquid removed through the toilet hatch 173 contains a certain amount of suspended solids, which can be separated from this portion of concentrated liquid and removed from the system using the secondary recirculation circuit 181.

For example, the concentrated liquid removed through the cesspool 173 can be fed through the secondary concentrated wastewater circuit 181 to one or more solids/liquid separation devices 183, such as a settling tank, a vibrating screen, a carousel vacuum filter, a horizontal belt vacuum filter , belt press, filter press and/or hydrocyclone.

After the suspended solids and liquid of the concentrated wastewater have been separated by the solids-liquid separator 183, the liquid portion of the concentrated wastewater without solid particles can be returned to the liquid sump 172 for further processing in a primary or secondary recirculation circuit connected to the concentrator.

The gas, from which liquid and suspended solids were removed when flowing through the gas washing unit 122, is supplied through a pipe or box from the back of the gas washing unit 122 (behind the corrugated filters 170) to the exhaust fan 190 of the exhaust unit 124 and is released into the atmosphere in the form of cooled gas , mixed with evaporated water. Of course, the exhaust fan is coupled to a motor 192 which forces the fan 190 to create a vacuum in the gas scrubber unit 122 to draw gas from the flare 130 through the heat transfer tube 140, the air pretreatment unit 119 and the concentrator unit 120. As indicated above with reference to FIG. 1, the exhaust fan 190 is only necessary to create a small vacuum in the gas scrubber unit 122 and thus ensure proper operation of the concentrator 110.

Although the speed of the exhaust fan 190 can be varied using a device such as a variable frequency drive to create different levels of vacuum in the gas scrubber unit 122 and operate over a range of gas flow rates and even draw all the gas from the flare 130 if there 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 purge unit 122 itself. To ensure its proper operation, the gas flowing through the gas purge unit 122 must have a sufficiently large (minimum required) velocity at the entrance of the gas purge unit 122. Usually this requirement performed 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 rotation speed 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 scrubbing unit 122 is provided with a gas recirculation loop, which can be used to ensure that sufficient gas is supplied to the inlet of the gas scrubbing unit 122 and to create the necessary pressure drop in the gas scrubbing unit 122. In particular, the gas recycling circuit includes a reverse a gas line or 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 nozzle of the gas purge unit 122 (for example, with the gas inlet nozzle of the gas purge unit 122), and the damper or adjustment mechanism 198, located in the return channel 196, which is designed to open and close the return channel 196 to establish communication of the high-pressure side of the exhaust unit 124 with the inlet of the gas purge unit 122. During operation, when the gas supply to the gas purge unit 122 is not large enough to provide the minimum necessary pressure drop in the purge unit 122, a damper 198 (which may be, for example, a gas valve or a louver) is open to allow gas from the high pressure side of the exhaust unit 124 (ie, gas that has passed through the exhaust fan 190) back to the inlet of the purge unit 122. This operation ensures that sufficient gas is supplied to the inlet of the gas purge unit 122 so that the exhaust fan 190 can provide the minimum necessary pressure drop in the gas purge unit 122.

In fig. 6 shows a particularly useful feature of the compact liquid concentrator 110 shown in FIG. 3, which consists in the presence of a group of easily openable inspection hatches 200, which can be used to penetrate inside the concentrator 110 for the purpose of its cleaning and inspection. Although in fig. 6 shows easy-to-open hatches 200 on one side of the gas purge unit 122, a similar group of hatches can be located on the other side of the gas purge unit 122, and a similar hatch is on the face of the submerged elbow 164, as shown in FIG. 5. As shown in fig. 6, each of the easily open inspection hatches 200 on the gas purge unit 122 includes a hatch cover 202, which may be a flat metal plate suspended from the gas purge unit 122 by two hinges 204, and the hatch cover 202 can be closed and opened by pivoting on the hinges 204. on the edges of the hatch cover 202 there are a number of quick-opening locks 206, designed to fix the hatch cover 202 in the closed position and to close the hatch cover 202 during the operation of the gas washing unit 122. In the embodiment shown in fig. 6, each hatch cover has eight quick release latches 206 located around each hatch cover 202, although any number of such quick release latches 206 may be used.

In fig. 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 purge unit 122 and is mounted on supports 209 located between the hatch frame 208 and the outer wall of the gas purge unit 122. A gasket 210 is installed around the opening in the hatch frame 208, which can be made of rubber or other compressed material. A similar additional or main gasket can be installed around the perimeter on the inside of the hatch cover 202, to improve the sealing quality when the hatch 200 is in a closed state.

Each quick-open latch 206, which is shown in an enlarged view in FIG. 8, has a handle 212 and a catch 214 (in this case in the form of a metal O-bracket) mounted on a hinged axis 216 passing through the handle 212. The handle 212 is mounted on another hinged axis 218 mounted on the outer wall of the hatch cover 202 with fastening bracket 219. When the handle 212 is moved up and rotated around the other hinge axis 218 (from the position shown in Fig. 8), the latch 214 is displaced along the outer wall of the gas washing unit 112 (when the hatch cover 202 is in the closed position), and the latch 214 can unhook 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 the other pivot axis 218, and therefore the hatch cover 202 to the hatch frame 208. When all quick-opening locks 206 are closed, the hatch cover 202 is pressed against the hatch frame 208, and the gasket 210 ensures their tight connection. Thus, closing all eight quick-open latches 206 on a particular hatch 200, as shown in FIG. 6, ensures reliable and tight closing of the hatch 200.

The use of easy-to-open hatches 200 replaces covers with holes and many bolts extending from the outer wall of the hub, which pass through these holes in the cover and are tightened with nuts to press the cover against the wall of the hub. Although a similar nut-bolt mounting mechanism, which is widely used in liquid concentrators to provide access to the interior of the concentrator, is very reliable, it takes a lot of time and effort to remove and install the removable cover. Easy opening hatches 200 with quick opening locks 206 shown in fig. 6, can be used in this case also because, since the pressure inside the gas purge unit 122 is less than the external pressure, a vacuum is created inside the gas purge unit 122, for which there is no need to tighten the bolts and nuts of the removable panel. It will be appreciated that the hatch configuration 200 allows the hatches 200 to be easily opened and closed with minimal effort and without the use of tools, thereby providing quick and easy access to equipment inside the gas scrubber unit 122, such as baffle plate 169 or replaceable filters 170, or to other parts of the hub 110, which are behind the inspection hatch 200.

As shown in fig. 5, the front wall of the submerged elbow 164 of the concentrator unit 120 also has an easily openable inspection hatch 200 that provides easy access to the interior of the flooded elbow 164. However, similar easily openable inspection hatches can be located on any part of the fluid concentrator 110 as needed, since most elements of the hub 10 works under rarefaction.

The combination of features shown in fig. 3-8 is typical of a compact liquid concentrator 110 that utilizes the waste heat of gas produced by flaring organic waste gas, waste heat that would otherwise be vented directly to the atmosphere. It is important to note that the concentrator 110 uses only a minimal amount of expensive material with high temperature resistance to manufacture from it the pipes and structural equipment necessary when working with high-temperature gases coming from the torch 130. In particular, the length of the heat transfer pipe 140, which is made of the most expensive materials, is minimized, which reduces the cost and weight of the liquid concentrator 110. In addition, due to the small size of the heat transfer pipe 140, only a minimum number of scaffolds in the form of a support rack 142 is needed, which further reduces the costs of constructing the concentrator 110. In addition, the air pretreatment unit 119 is located directly on the concentrator block 120 and the gas in these blocks enters from top to bottom, which allows you to install these concentrator blocks 110 directly on the ground or on a sled. Further, this configuration allows the hub 110 to be placed very close to the torch 130, making it more compact. Similarly, this configuration allows high-temperature concentrator units 110 (eg, torch top 130, heat transfer pipe 140, and air pretreatment unit 119) to be placed above the ground without having to worry about accidental contact, resulting in a higher level of safety. In fact, due to the rapid cooling that occurs in the venturi section 162 of the concentrator unit 120, both the venturi section 162 itself, the flooded elbow 164, and the gas scrubber unit 122 usually cool enough to be touched without fear of burning ( even if at the exit from the torch 130 the gas had a temperature of 982 72). Rapid cooling of the gas-liquid mixture allows the use of materials of lower cost, which are easy to manufacture and which are characterized by corrosion resistance. Additionally, components downstream of flooded elbow 164, such as gas scrubber unit 122, exhaust fan 190, and exhaust unit 124, will be made of materials such as fiberglass.

The liquid concentrator 110 is also a very fast concentrator. Because the concentrator 110 is a direct contact concentrator, it is not subject to sedimentation, clogging, or clogging to the degree that most other concentrators are. Further, the ability to adjust the operation of the flare by opening and closing the flare cap 134 allows continuous use of the flare 130 for burning gas from organic waste regardless of whether the concentrator 110 is operating or not, without stopping its operation during the start and stop of the concentrator 110. In particular, the flare the cap 134 can be quickly opened at any time so that the flare 130 can simply burn the organic waste gas as it normally does when the concentrator 110 is shut down. Alternatively, the flare cap can be quickly closed at the time the concentrator 110 is started and thus directed all the hot gases that are generated in the torch 130 into the concentrator 110, which allows the concentrator 110 to start operation without stopping the torch 130. In any case, the concentrator 110 can be started and stopped by only changing the position of the flare cap 134, but without stopping the operation of the torch 130 .

If necessary, during operation of the concentrator 110, the flare cap 134 can be partially opened to adjust the amount of gas supplied from the flare 130 to the concentrator 110. This gas supply adjustment, in conjunction with the adjustment of the atmospheric air inlet valve, can be used to adjust the gas temperature at the site inlet. with a venturi profile of 162.

In addition, due to the compact configuration of the air pretreatment unit 119, the concentrator unit 120, and the gas scrubber unit 122, individual parts of the concentrator unit 120, the gas scrubber unit 122, the exhaust fan 190, and at least the lower part of the exhaust unit 124 can be stationary installed (attached and used as support) on the sled or plate 230, as shown in fig. 2. The upper part of the concentrator unit 120, the air pretreatment unit 119 and the heat transfer pipe 140, as well as the upper part of the exhaust pipe can be removed and placed on the sled or on the plate 230 during transportation, or they can be transported in a separate truck. Due to the way the lower parts of the hub 110 will be installed on the sled or plate, the hub 110 is easy to remove and install. In particular, during the installation of the concentrator 110, the sled 230, on which the gas purge unit 122, flooded elbow 164 and exhaust fan 190 are installed, can be unloaded at the place where the concentrator will be used, simply by unloading them from the sled 230 to the ground or to another storage area, on which hub 110 will assemble. The venturi section 162, cooler 159, and air pretreatment unit 119 will then be placed on top and attached to the submerged elbow 164. The pipe 150 can then be extended upward to match the height of the flare 130 to which the hub 110 is to be attached. In some cases, it may first, the torch-cap unit 132 is installed on the already existing torch 130. After that, the heat transfer pipe 140 can be raised to the appropriate height and fixed between the torch 130 and the unit for pre-treatment of air 119, installing the support rack 142 in place. For concentrators with an evaporative capacity of 38000 or more up to 114,000 liters per day, it is possible for the entire flare assembly 115 to be mounted on the same sled or plate 230 on which the concentrator 120 is mounted.

Since most of the pumps, pipes, sensors, and electronic equipment are located or connected to the concentrator unit 120, gas scrubber unit 122, or exhaust pump 190, installing the concentrator 110 in a designated location will not require a lot of piping 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 designated location. In addition, since most of the components of the hub 110 are stationary mounted on the sled 230, the hub 110 will be easily transported by truck or other vehicles and can easily be unloaded and installed at a specific location, such as an area near a landfill flare.

In fig. 9 shows a control scheme 300 that can be used for the hub 110 shown in FIG. 3. As shown in fig. 9, the control system 300 includes a controller 302, which may be a digital signal processor type controller, a programmable logic controller which may, for example, perform control based on multistage logic, or some other type of controller. The controller 302 is connected, of course, to various components in the hub 110.

In particular, the controller 302 is connected to the drive motor 135 of the flare cap 134, which performs the opening and closing of the flare cap 134. The drive motor 135 can be used to adjust the position of the flare cap 134, 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 torch cap 134 to any of a number of intermediate positions ranging from a fully open position to a fully closed position. If necessary, the motor 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 atmospheric air intake valve 306 located in FIG. From the air pretreatment unit 119 before the venturi section 162, and can be used to control the pumps 182 and 184, which regulate the amount and ratio of the injection of the new fluid that has entered the concentration and the recycle fluid that is being processed in the concentrator 110. Controller 302 can be connected to a level sensor

317 in the liquid sump (eg, to a float sensor, a non-contact sensor such as a radar or acoustic sensor, or a differential pressure sensor) The controller 302 can use the signal received from the level sensor 317 in the liquid sump to control the pumps 182 and 184 and maintain the level of the concentrated liquid in the liquid sump 172 corresponding to a predetermined or required value. The controller 302 may also be connected to the 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 frequency-controlled motor, the frequency of which is changed to control the speed of rotation of the fan. In addition, the controller 302 is connected to a temperature sensor 308 located, for example, at the inlet of the concentration unit 120 or at the inlet of the section with a venturi profile 162, and receives a temperature signal generated by the temperature sensor 308.

The temperature sensor 308 may also be located behind the venturi section 162 or the temperature sensor 308 may include a pressure sensor generating a pressure signal.

During operation and, for example, at concentrator 110 start-up, when the flare 130 continues to operate and thus burns organic waste gas, the controller 302 must first turn on the exhaust fan 190 to create a vacuum in the scrubber unit 122 and the concentrator unit 120. After that, either at the same time, the controller 302 signals the motor 135 to close the flare cap partially or completely and direct the waste heat from the flare 130 into the heat transfer pipe 140 and thus into the air pretreatment unit 119. By receiving the temperature signal from the temperature sensor 308, the controller 302 can adjust atmospheric air inlet valve 306 (typically partially or fully closed) and/or flare cap actuator to adjust gas temperature at the inlet of concentrator unit 120. Generally speaking, atmospheric air inlet valve 306 is actuated to the fully open position by a biasing member such as a spring , (that is, can be a normally open valve), and the controller 302 can begin to close the valve 306 to regulate the amount of atmospheric air supplied to the air pretreatment unit 119 (by creating a vacuum in the air pretreatment unit 119), and thus bring the mixture of atmospheric air and hot gases from the torch 130 to the desired temperature . If necessary, the controller 302 can also adjust the position of the flare cap 134 (setting it anywhere between the fully open and fully closed positions) and can vary the speed of the exhaust fan 190 to adjust the amount of gas entering the air pretreatment unit 119 from of the flare 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 coming out of the flare 130.

Therefore, the controller 302 will regulate the temperature and amount of gas flowing through the concentrator unit 120 by changing one or more parameters, in particular the degree of closure of the atmospheric air inlet valve 306, the position of the flare cap 134 and the speed of the exhaust fan 190, for example, according to the results of the measurement of the temperature sensor 308 at the inlet of the concentrator unit 120. This feedback system is necessary because in many cases the air exiting the torch 130 has a temperature in the range of 649°C to 982°C, which is very high or exceeds the value that it will have to ensure the efficient operation of the hub 110.

In any case, as shown in fig. 9, the controller 302 can also be connected to a motor 310 that will change the position of the venturi plate 163 in the narrowed area of the concentrator unit 120 to regulate the level of turbulence created by the concentrator unit 120. And the controller 302 can control the operation of the pumps 182 and 184 to vary the rate (and rate ratio) at which pumps 182 and 184 deliver circulating fluid and new wastewater to cooler inlets 159 and venturi sections 162. In one embodiment, controller 302 may adjust the ratio of circulating fluid to new fluid at a level of 10: 1, so that while pump 184 supplies fresh fluid to inlet port 160 at a rate of 30.4 liters per minute, recirculation pump 182 supplies concentrated fluid at a rate of 304 liters per minute. Instead, or additionally, the controller 302 can regulate the flow of new liquid entering the concentrator (by the pump 184 ) for processing, maintaining the same or a predetermined level of the amount of concentrated liquid in the liquid sump 172 , for example, using a level sensor 317 .

Of course, the amount of liquid in the liquid sump 172 will depend on the rate of concentration in the concentrator, the rate at which the concentrated liquid is pumped out by the pump or supplied to the liquid sump 172 via a secondary recirculation circuit, and the rate at which the pump 182 feeds liquid from the sump. for liquid 172 in the concentrator on the primary recirculation circuit.

If necessary, the atmospheric air inlet valve 306 or the flare cap 134, individually or together, can be in an open position that provides a safety, such that the flare cap 134 and the atmospheric air inlet valve 306 open in the event of a system malfunction (eg, no control signal ) or disconnection of hub 110. In one case, flare cap motor 135 may be biased or biased by a squeeze member, such as a spring, to hold flare cap 134 in an open position or to cause flare cap 134 to open after de-energizing motor 135. Alternatively, the squeeze member may be a counterweight 137 of the torch cap 134, which can be located in such a position that the torch cap 134 itself moves to the open position under the action of the counterweight 137, when the motor 135 is de-energized or the control signal is lost. As a result, the flare cap 134 quickly opens when the power is cut off or when the controller 302 opens the flare cap, allowing hot gas to escape from the flare 130 through the top opening. Of course, it is possible to use other methods of transferring the flare cap 134 to the open position in the absence of a control signal, in particular with the help of 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 during the reduction of pressure in the cylinder opens the torch cap 134 in the absence of a control signal.

As stated above, the flare cap 134 and the atmospheric air inlet valve 306 operate in synchronism to protect the construction materials used in the concentrator 110 and, once the system shuts down, the flare cap 134 and the atmospheric air inlet valve 306 will immediately automatically open, thereby preventing the hot gas, which is formed in the torch 130, 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 will similarly be spring-loaded or otherwise biased to open when the concentrator 110 is turned off or in the absence of a control signal applied to the valve 306. This allows the air pre-treatment unit 119 and the concentrator unit 120 to be rapidly cooled through open flare cap 134. In addition, by quickly opening the atmospheric air valve 306 and the flare cap 134, the controller 302 can quickly shut down the concentrator 110 without disabling or affecting the operation of the flare 130.

Next, as shown in fig. 9, the controller 302 will be connected to the venturi motor 310 or any other actuator that rotates or positions the venturi 163 at a certain angle in the area with the venturi profile 162. Using the motor 310, the controller 302 can change the angle of the venturi 163 to adjust the flow of gas through the concentrating unit 120 and thus change the nature of the turbulent flow of gas flowing through the concentrating unit 120, aiming for 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 inclination of the venturi plate 163 to achieve the optimal concentration of the wastewater. It is clear 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 atmospheric air inlet valve 306 and the speed of the exhaust fan 190 to maximize the degree of concentration (turbulent mixing) of the wastewater, avoiding complete evaporation of the water and thus preventing the formation of solid particles. The controller 302 may use the pressure input signals from the pressure sensors to select the position of the venturi plate 163. Of course, the venturi plate 163 may be adjusted either manually or automatically.

The controller 302 can also be connected to a motor 312 that regulates the operation of the damper 198 in the gas recirculation circuit of the gas scrubbing unit 122. The controller 302 can cause the motor 312 or another type of actuator to move the damper 198 from a closed position to an open or partially open position, for example, on signals from pressure sensors 313, 315, located at the gas inlet and outlet from the gas washing unit 122. The controller 302 can set the valve 198 in such a position that the gas flows from the high pressure side of the exhaust unit 124 (behind the exhaust fan 190) to the inlet of the gas washing unit so that maintain a predetermined minimum pressure drop between the two pressure sensors 313, 315. Maintaining the minimum pressure drop ensures the proper operation of the gas purge unit 122. Of course, the damper 198 can be adjusted manually or use electric control.

Thus, it follows from the foregoing that the controller 302 may provide one or more closed/open control loops used to start or stop the concentrator 110 without disrupting the operation of the flare 130. For example, the controller 302 may provide a flare cap control loop that opens or closes flare cap 134, an air valve control circuit that opens or begins to open the atmospheric air intake valve 306, and an exhaust fan control circuit that starts or stops the exhaust fan 190 depending on whether the hub 110 is started or stopped. Additionally, during operation, the controller 302 may create one or more real-time control loops that may adjust various elements of concentrator 110 individually or in combination with each other to improve or optimize the concentrator process. By creating these real-time control loops, the 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 air inlet valve shut-off member 306 to regulate the flow of fluid flowing through concentrator 110, and/or air temperature at the entrance to the concentrator unit 120 based on signals from temperature and pressure sensors. In addition, the controller 302 can provide steady-state performance of the concentrator by controlling the pumps 184 and 182 that supply fresh and circulating fluid to the concentrator unit 120. Also, the controller 302 can provide a pressure control loop to adjust the position of the damper 198 to ensure proper operation of the gas scrubbing unit 122. Of course, although the controller 302 shown in FIG. 9 in the form of a separate control device that creates different control loops, the controller 302 can be a number of different control devices, for example, a number of different programmable logic controllers.

It is understood that the concentrator 110 proposed herein directly utilizes the hot gaseous emissions in the process processes after these gaseous emissions have been thoroughly treated to meet the requirements of the gaseous emission standards, and thus definitely meet the operational requirements of the process that generates the waste heat, and a method that uses waste heat in a simple, reliable and efficient way.

In addition to being an essential component of the concentrator 110 during its operation, the flare cap 134 described herein, whether automatically or manually actuated, may be used in a stand-alone mode of operation to provide weather protection for the flare itself or the flare-concentrator assembly when the flare is not operating. . Closed by the torch cap 134, the internal equipment of the metal body of the torch 130 together with its lining, burners and other important components of the torch installation 115 and the heat transfer unit 117 is protected from corrosion and general wear associated with the impact on these components. In this case, the controller 302 can control the motor 135 of the torch cap 134, setting it to a fully open or partially open state during the operation of the torch 130 at idle. In addition, in addition to using a torch cap 134 that automatically closes when the torch 130 is turned off and automatically opens when the torch 130 is ignited, a small burner such as a conventional lighter can be installed inside the torch 130, which can burn when the torch 130 is turned off and torch cap 134 is closed. This small burner further helps protect torch components from moisture wear by keeping the torch 130's internals dry. An example of a stand-alone flare that may use the flare cap 134 described herein in stand-alone operation is a stand-alone flare installed in a landfill to regulate the gas content of the air when the biogas-fired power plant is shut down.

Although liquid concentrator 110 has been described above as connected to an organic waste gas flare to utilize waste heat from that flare, liquid concentrator 110 can easily be connected to other waste heat sources. For example, in fig. 10 shows a liquid 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 implementation, the engine in the power plant 400 may run on organic waste gas to generate electricity, the concentrator 110 may also be connected to the exhaust pipe of other types of engines, particularly engines of the type that run on gasoline or diesel fuel.

In fig. 10 exhaust gases generated in the engine (not shown) in the power plant 400 enter a muffler 402 outside the power plant 400, and from there into an exhaust pipe 404 equipped with an exhaust cap 406 on top. The cap 406 is equipped with a counterweight so that it can close the exhaust pipe 404 when there is no exhaust gas in the pipe 404, but is easily opened by the exhaust gas coming out of the pipe 404. In this case, the exhaust pipe 404 has a U-shaped connector designed to connect the pipe 408 to the heat transfer pipe 408, by in which the exhaust gas (source of waste heat) enters the expansion section 410 from the engine. The expansion section 410 is connected to the cooler 159 of the concentrator 110 and directs the exhaust gas from the engine directly into the concentrator unit 120 of the concentrator 110. When using engine exhaust gases as a source of waste heat, it is usually not it is necessary to install an atmospheric air inlet valve before the concentrating unit 120, since the exhaust gas on leaving the engine usually has a temperature lower than 482 "C, so it does not have to be cooled too much before entering the cooler 159.

The remaining parts of the hub 110 are the same as described above with reference to FIG. 3-8. As a result, it can be seen that the liquid concentrator 110 can be easily adapted to use a wide variety of waste heat sources without making significant changes to the design.

Typically, when controlling the fluid concentrator 110 shown in FIG. 10, the controller turns on the exhaust fan 190 when the engine at the power plant 400 is running. The controller increases the speed of the exhaust fan 190 from the minimum value until most or all of the exhaust gases are fed from the pipe 404 into the heat transfer pipe 408 instead of exiting the exhaust pipe 404 to the atmosphere. It is not difficult to determine when such an operating mode will be reached, it corresponds to the moment when, when the speed of the exhaust fan 190 increases, the cap 406 first sits on the top of the exhaust pipe 404. It is important not to allow a further increase in the speed of the exhaust fan 190, which creates a mode greater than vacuum in the concentrator 110 is required to ensure that the operation of the concentrator 110 does not result in a change in back pressure and, in particular, in the creation of undesirable levels of suction experienced by the engine in the power plant 400. A change in back pressure or the creation of a suction in the exhaust pipe 404 can adversely affect combustion of fuel in the engine, which is undesirable. In one embodiment, the controller (not shown in Fig. 10), as a programmable logic controller, can use a pressure sensor installed in the pipe 404 near the cap 406 to continuously monitor the pressure at this location. The controller can then provide a signal to the variable frequency drive on the exhaust fan 190 to regulate the speed of the exhaust fan 190, maintain the pressure at a set level and thus prevent unwanted back pressure or suction from acting on the engine.

In fig. 11 and 12 show a cross-sectional side view and a cross-sectional top view of another embodiment of the liquid concentrator 500. The concentrator 500 is installed in a vertical position. However, the hub 500 shown in FIG. 11, will be located in a horizontal position or in a vertical position, depending on the specific restrictions imposed when used for a specific purpose. For example, a truck-mounted modification of the concentrator can be in a horizontal position so that the concentrator can pass under bridges and overpasses during transport from place to place.

The liquid concentrator 500 has a gas inlet nozzle 520 and a gas outlet hole 522. The gas inlet nozzle 520 and the gas outlet hole 522 are connected by a flow channel 524. The flow channel 524 has a narrowed section 526, which accelerates the passage of gas through the flow channel 524. Before the narrowed section 526, liquid is injected into the gas flow through the nozzle 530. Unlike the embodiment shown in fig. 1, in the embodiment shown in fig. 11, the narrowed section 526 directs the gas-liquid mixture into the cyclone chamber 551. The cyclone chamber 551 enhances the mixing of the gas and liquid while simultaneously acting as a mist trap shown in FIG. 1. The gas-liquid mixture is fed into the cyclone chamber 551 tangentially (see Fig. 12), and then moves through the cyclone chamber 551 like air in a cyclone in the direction of the liquid removal area 554. The cyclonic vortex is enhanced by the hollow cylinder 556 located in the cyclone chamber 551, through which the gas enters the gas outlet 522. The hollow cylinder 556 is a physical barrier that provides cyclonic vorticity throughout the cyclone chamber 551, including the area for liquid removal 554.

When the gas-liquid mixture passes through the narrowed section 526 of the flow channel 524 and circulates in the cyclone chamber 551, then part of the liquid evaporates and is absorbed by the gas. Centrifugal force then accelerates the movement of liquid droplets entrained by the gas towards the side wall 552 of the cyclone chamber 551, where the entrained liquid droplets coalesce, forming a film on the side surface 552. At the same time, the centrifugal forces created by the exhaust fan 550 collect the gas released from the droplets at the inlet 560 of the cylinder 556 and direct it to the gas outlet 522. Thus, the cyclone chamber 551 acts both as a mixing chamber and as a mist capture chamber. When the liquid film flows in the chamber in the direction of the area for liquid removal 554 under the combined action of gravity and vortex motion in the cyclone chamber 551 in the direction of the area for liquid removal 554, the gas constantly circulating in the cyclone chamber 551 also evaporates part of the liquid film. When the liquid film flows to the liquid discharge section 554 from the cyclone chamber 551, the liquid enters the recirculation circuit 542.

Similarly, the liquid circulates through the concentrator 500 until the desired degree of concentration is achieved. A portion of the concentrated sludge can be withdrawn through the cesspool 546 when the sludge has reached the required level of concentration (this method is called purging). Fresh liquid is introduced into the circuit 542 through the fresh liquid inlet 544 at a rate equal to the sum of the evaporation rate and the sludge removal rate through the toilet hatch 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 under the action of the exhaust fan 550 and in the direction of the inlet opening 560 of the hollow pipe 556. The purified gas then enters the hollow pipe 556 and, finally, it is released through the gas outlet 522 into the atmosphere or submitted for further processing (for example, for oxidation in a flare).

In fig. 13 is a diagram of a distributed fluid concentrator 600 that is configured to allow the concentrator 600 to be used with multiple waste heat sources of various types, even waste heat sources located in locations that are difficult to access, such as from the sides of buildings, among various types other equipment, away from roads or other access routes.

Although the liquid concentrator 600 described here is used to treat and concentrate leachate, such as leachate collected at a landfill, the liquid concentrator 600 can be used to concentrate other types of liquids as well, including many different wastewaters.

Generally speaking, the fluid concentrator 600 includes a gas inlet 620, a gas outlet or gas outlet 622, a flow channel 624 that extends from the gas inlet 620 to a gas outlet 622, and a fluid recirculation system 625. The concentrator unit includes a flow channel 624 that includes a cooling section 659, which includes a gas inlet 620 and a liquid inlet 630, a venturi section 626 located downstream of the cooling section 659, and a discharge or exhaust fan 650 connected downstream of the venturi section 626. The fan 650 and a submerged elbow 654 connect the gas outlet of the concentrator block (for example, the exhaust nozzle of the section with a venturi profile 626) to the pipeline 652. In this case, the submerged elbow 654 provides a rotation of the flow channel 624 by 90 degrees. If necessary, the submerged elbow 654 can provide a turn to an angle that is less than or greater than 90 degrees. Pipeline 652 is connected to a mist trap, shown in this case as a cross-flow gas scrubber 634, which in turn is connected to a chimney 622A having a gas outlet 622.

The recirculation system 625 includes a liquid sump 636 connected to the liquid outlet of the cross-flow gas scrubber 634, and a recirculation pump 640 connected between the liquid sump 636 and a conduit 642 that supplies the circulating liquid to the liquid inlet 630. The feeder 644 also supplies filtrate or what another liquid to be treated (eg, a concentrated liquid) into the liquid inlet 630 so that it enters the cooler 659. The recirculation system 625 also includes a liquid outlet 646 connected to the conduit 642, which supplies a certain amount of circulating liquid (or concentrated liquid) into tank 649 for storage, settling and recirculation. Heavier or more concentrated portions of liquid in settling tank 649 sink to the bottom of tank 649 as sludge, which is removed and transported for removal in concentrated form. Less concentrated portions of liquid from reservoir 649 are fed back to liquid sump 636 for reprocessing and further concentration, as well as to ensure at all times a proper supply of liquid to inlet 630 and thus prevent the formation of dry particles. Dry particles can be formed with a reduced ratio of the volume of the treated liquid to the volume of hot gas.

During operation, the cooler 659 mixes the liquid that has entered from the liquid inlet port 630 with the gas that contains the waste heat collected, for example, from the engine muffler and the exhaust pipe 629 associated with the internal combustion engine (not shown in the figure). The liquid from the liquid inlet valve 630 is, for example, a filtrate to be processed or concentrated. As shown in Fig. 13, the cooler 659 is attached in a vertical position above the venturi section 626, which contains a narrowed section that accelerates the flow of gas and liquid through the flow channel 624 immediately behind the venturi section 626 and in front of the fan 650. Of course, the fan 650 serves to create a vacuum immediately behind the venturi section 626, to draw gas from the exhaust pipe 629 through the venturi section 626 and the flooded elbow 564 to provide mixing of the gas and liquid.

As indicated above, the cooler 659 receives hot exhaust gas from the engine exhaust pipe 629 and will be attached directly to any desired section of the exhaust pipe 629. In this exemplary embodiment, the engine exhaust pipe 629 is mounted outside of the building 631 that houses one or more generators that produce electricity using gas from organic waste as fuel. In this case, the cooler 659 will be connected directly to a device for removing condensate (eg, a condensation pot) connected to the exhaust pipe 629 (ie, to the bottom of the exhaust pipe 629). Here, the cooler 659 will be mounted directly under or next to the pipe 629, so that only a few inches or at least a few feet of expensive high temperature pipe is needed to connect 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 a suitable elbow or branch.

As noted above, liquid to be vaporized (e.g., landfill leachate) is injected through inlet 630 into flow channel 624 through cooler 659. If desired, liquid inlet 630 may include a variable nozzle for atomizing liquid in cooler 659. Liquid inlet 630, regardless of whether it is provided with a nozzle or not, can inject liquid in any direction, both perpendicular to the gas flow and parallel to the gas flow moving along the flow channel 624. In addition, when the gas (and waste heat contained in in it) and the liquid pass through the section with the Venturi profile 626, according to the Venturi principle, the flow rate increases and a turbulent flow is formed, which completely mixes the gas and liquid in the flow channel 624 directly behind the section with the Venturi profile 626. As a result of mixing in the turbulent mode, part of the liquid quickly evaporates and becomes part of the gas stream. Evaporation uses a large amount of heat energy from the waste heat 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 turns at an angle of 90 degrees, changing the vertical direction of flow to the horizontal direction of flow. The gas-liquid mixture flows around the fan 650 and is fed into the high-pressure region on the discharge side of the fan 650, the high-pressure region being located in the pipe section 652. The use of the flooded elbow 654 at this point in the system is necessary for at least two reasons. First, the fluid in the lower part of the flooded elbow 654 reduces erosion at the turning point of the flow channel 624, which is usually caused by particles suspended in the gas-liquid mixture, which would enter the 90-degree bend at high speed and strike at a steep angle directly into the the lower surface of a conventional elbow if the submerged elbow 654 were not used... The fluid in the lower part of the submerged elbow 654 absorbs the energy of these particles and thus protects the lower surface of the submerged elbow 654 from erosion. In addition, the liquid droplets still contained in the gas-liquid mixture in the flooded elbow coalesce much more easily and move away from the flow if they hit the liquid. That is, the liquid at the bottom of the flooded elbow 654 is used to trap the liquid droplets that impinge on it, since the liquid droplets contained in the flow are retained much more easily if these sprayed liquid droplets are in contact with the liquid. Thus, the flooded elbow 654, which may have a liquid outlet (not shown), for example, to the recirculation circuit 625, serves to remove some of the process liquid droplets and condensate from the gas-liquid mixture leaving the venturi section 626.

It should be noted that the gas-liquid mixture flowing through the venturi section 626 rapidly approaches the adiabatic saturation point, which is at a temperature much lower than the temperature of the gas at the outlet of the exhaust pipe 629. For example, although the gas at the outlet of the exhaust pipe 629 may to have a temperature in the range of 482 "C to 982 "C, the gas-liquid mixture in all sections of the concentration system 600 by section with a venturi profile 626 will typically have a temperature in the range of 66 "C to 87.8 "C, although the temperature of the mixture will be higher, and lower than this temperature range depending on the operating parameters of the system. As a result, the section of the concentration system 600 behind the section with the venturi profile 626 does not need to be made of temperature-resistant materials and does not need to be insulated at all, or can be insulated only to the extent necessary for the transportation of gases with an elevated temperature, if the insulation is carried out for the purpose of more complete utilization of waste heat, which contained in the hot gas And also the sections of the concentration system 600 by 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 safety threat, or need only minimal external protection. In particular, sections of the concentration system 600 behind the venturi section 626 may be made of fiberglass and may require only minimal or no insulation. It should be noted that the gas-liquid stream can be fed through sections of the concentration system 600 beyond the venturi section 626 for a relatively long distance while still remaining close to the adiabatic saturation point, and thus allowing it to be easily transported by conduit 652 from the building 631 to a more accessible location where another the equipment associated with the hub 600 can be placed in a conventional manner. In particular, the pipe section 652 can extend for 6 meters, 12 meters, or even a greater distance, although the flow still remains in a state close to adiabatic saturation. Of course, these distances will be more or less dependent on, for example, the ambient temperature, the type of piping used, or the presence of insulation. Additionally, since the conduit section 652 is located on the high pressure side of the fan 650, it is easy to remove condensate from this flow. In the embodiment shown in fig. 13, a section of conduit 652 is shown to wrap around the air cooler or pass under the air cooler connected to the motors within the building 631. But the air cooler in FIG. 13 is just one of the options for those obstacles that can be found near the building 631 and which do not allow placing all the 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 structures, inaccessible territory without roads and convenient approaches.

In any case, the pipeline section 652 directs the gas-liquid flow to a state close to the adiabatic saturation point in the fog trap 634, which would be, for example, a cross-flow gas scrubber. The mist catcher 634 serves to remove carried liquid droplets from the gas-liquid flow. The separated liquid is collected in the liquid sump 636, from where it enters the pump 640. The pump 640 feeds the liquid through the return line 642 of the recirculation circuit 625 into the liquid inlet 630. Thus, the separated liquid can be further concentrated by evaporation to the required concentration level and/ or served to prevent the formation of dry particles. Fresh liquid is supplied for concentration through the fresh liquid inlet 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 during the passage of the gas-liquid mixture through the flow channel 624 and the rate of withdrawal of liquid or sludge from the settling tank 649 (provided that the level of liquid in the settling tank 649 does not change). In particular, part of the liquid can be removed through the toilet hatch 646 when the liquid in the recirculation circuit 625 reaches the required degree of concentration. Part of the liquid diverted through the toilet hatch 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, a liquid part and a semi-solid part). The semi-solid can be scooped out of the 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 pushes the gas through another section of the flow channel 624, which is under increased pressure. Cooler 659, venturi section 626, and fan 650 will be attached to building 631 using any type of connector and may be in close proximity to the waste heat source. However, the mist trap 634 and gas outlet 622, as well as the sump tank 649, may be located some distance from the cooler 659, venturi section 626, and fan 650, for example, in an easily accessible location. In one embodiment, the fog trap 634 and gas outlet 622, as well as the sump tank 649 can be mounted on a mobile platform, such as a liquid sump or trailer frame.

In fig. 14-16 shows 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 be used for fluid concentration in that position, while other components may be removed and installed near the waste heat source as shown in the embodiment shown in FIG. 13. The liquid concentrator 700 has a gas inlet port 720 and a gas outlet port 722. The gas inlet port 720 communicates with the gas outlet port 722 through a flow channel 724. The flow channel 724 has a narrowed section or a section with a venturi profile 726 that increases the speed of gas flow through the flow channel 724. The gas is drawn into the cooler 759 with an exhaust fan (not shown in the pictures). A liquid is injected into the gas stream in the cooler 759 through the liquid inlet pipe 730. The gas is fed from the venturi section 726 to the fog catcher (or cross-flow gas scrubber) 734 through the elbow 733. From the fog catcher 734, the gas is fed to the gas outlet 722 through the pipe 723. Of course, as noted above, some of these components can be removed from the frame and installed directly adjacent to the waste heat source, while other components (such as mist trap 734, pipe 723, and gas outlet 722) can remain on the frame.

When the gas-liquid mixture passes through the section with the Venturi profile 726 of the flow channel 724, a part of the liquid evaporates and is absorbed by the gas, spending a large part 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 composition of the exhaust gas.

In the embodiment shown in fig. 14-16, parts of the liquid concentrator 700 can be disassembled and mounted on a liquid sump or truck trailer for transport.

For example, the cooler 759 and venturi section 726 can be removed from the elbow 733, as shown in FIG. 14 with a dotted line. In a similar way, the pipe 723 can be removed from the fan 750, as shown in fig. 14 with a dotted line. Elbow 733, mist trap 734, and exhaust fan 750 can be mounted on a liquid sump or truck trailer 799 as a single unit. Pipe 723 can be attached to liquid sump or truck trailer 799 separately. The cooling section 759 and venturi section 726 can also be mounted on a pallet or truck trailer 799 or transported separately.

Various modifications 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 this wastewater. Such changes will be particularly useful where the pollutants targeted for removal are co-located with substances whose emissions are normally regulated by government agencies. Examples of such pollutants would be sulfur oxides (SOx), which are usually present in the exhaust gas during the combustion of gas from organic waste, as well as ammonia (MNH3). Below 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 5Ox and MNH, but this description should not be limited to the removal of only these pollutants.

Removal of 5OHx

Hydrogen sulfide (H25) is a well-known poisonous gas that can be released during the bacterial decomposition (chemical reduction) of sulfur-containing substances, sulfites, and sulfates, and is present in landfill waste. After formation, H»Z combines with other gases formed as a result of bacterial action of all types occurring at the landfill, resulting in 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 (eg, gypsum wallboard material), which contributes 10,000 parts of Hg5 per million parts (wt) of gas from the organic waste. Hydrogen sulfide is a component of organic waste gas burned in a landfill flare, as described in this document, for example.

Combustion of NO5 in a gas flare, reciprocating engine or turbine is best, as NO5 will be converted to sulfur oxides (SO5OX), which avoids expensive organic waste gas pretreatment to remove H2a5. However, sulfur oxides may be considered an air pollutant in some countries. Another advantage of burning He5 in a flare is that H2e5 increases the amount of heat in the flare exhaust that will be used to concentrate the landfill leachate, reducing the total amount of fuel required.

Wet gas scrubbers are commonly used to remove Oxy from exhaust gases, which are formed during the combustion of fuels that contain sulfur compounds, including H2g5. Examples of such scrubbers include spray and packed columns contacting (wet contact) alkaline materials (such as solutions or catalyzed suspensions of sodium hydroxide, or lime (CaSO3)) directly with the exhaust gas intended to "clean" (i.e. remove) it

ZOh. The principle behind wet cleaning can be used in the context of the wastewater concentrator described in this document.

Alkaline material of known concentration can be added to the waste water in an amount sufficient to react with the OH present in the exhaust gas and convert it into sodium hydroxide and sodium sulfate (in which the alkali is Mahon) and calcium sulfate (Sabzo4) in which the alkali is lime. Once formed, the sulfite/sodium sulfate and calcium sulfate salts will be removed from the process as part of the liquid concentrate. Finally, the sulfite / sodium sulfate and calcium sulfate salts can be removed at chemical waste treatment plants, or further converted into a stream with a high solids content (for example, up to 100 95), which will be placed in special chambers at the landfill to prevent the reverse conversion of sulfite / sulfates into gas from organic waste, such as H25. Since the residual volume generated from landfill leachate is usually a highly diluted aqueous waste stream, typically only 5% of the original volume of wastewater even with added sulfite/sulfate salts, the costs of transportation and disposal at chemical waste treatment facilities outside of the work site, or the costs of building and operating special chambers at the landfill to contain 10095 solids, should be cost-effective, especially when compared with the costs of cleaning flue gas from emissions or removing hydrogen sulfide before combustion without using the waste heat of the combustion process as the main energy source for wastewater treatment (for example, leachates).

This dual-purpose use for the wastewater treatment system provides enormous benefits to landfill owners who find that emissions from flares or power plants using organic waste gas as fuel exceed the established limits for ZoXx emissions.

Converting a concentrator to operate in a combined concentration/gas purge mode involves only the addition of a dosing system (eg, a pump connected to the concentrator controller) and a supply tank for the selected alkaline reagent used for the gas purge. Also, operational changes to control the addition of a 5Ox removal step to the concentration process will not significantly increase the complexity of the simple analytical tests that will be used to control both the levels of hydrogen sulfide in the organic waste gas and the amount of sulfate in the concentrate produced by the process.

As can be seen in fig. 10, the concentrator unit 120 may include an inlet 187 for caustic (or alkaline) material coupled to a supply of caustic (or alkaline) material 193 (eg, sodium hydroxide or lime) using a feed line 189. A pump 191 may pressurize the feed line 189 of caustic or alkaline material from caustic or alkaline material supply tank 193 so that the caustic or alkaline material is injected into the concentration unit 120 (eg, through the venturi section 162) for mixing with the exhaust gas of the flare unit 130 or generator. In other embodiments, the caustic or alkaline material may be mixed with the filtrate in the filtrate feed line 186 before being fed to the concentration unit 120. Regardless of the method, after the caustic or alkaline material is fed to the concentration unit 120, the material is rapidly mixed with the exhaust gas in the concentration unit 120 together with the filtrate as described above. After mixing, the caustic or alkaline material reacts with the sulfur oxides, converting the sulfur oxides into sodium sulfate and sodium sulfite or calcium sulfate as described above. After conversion, the sodium sulfate, sodium sulfite, and/or calcium sulfate immediately pass into the liquid phase, where they either remain dissolved or precipitate from the gas-liquid mixture in the concentration unit 120. Thus, the sulfur that was originally in the form of He5 in gas from organic waste, passes into the liquid phase and finally enters together with the concentrated filtrate in the sump 172 of the fog trap unit 122 and can be removed together with the concentrated filtrate for further destruction. As shown in fig. 9, the controller 302 can be operatively connected to the pump 191 to control the dosing of the supply of caustic or alkaline material to the concentration unit 120.

The controller 302 can determine the correct dose of caustic feed based on at least the mass flow of the exhaust gas through the concentrating unit 120 and the percentage of sulfur oxides in the exhaust gas. Thus, this concentrator can indeed be adapted to different components in the exhaust gas and/or different exhaust gas mass flow rates. As a result, this concentrator has the ability to simultaneously concentrate landfill leachate and remove pollutants, such as sulfur oxides, from the exhaust gas of a landfill flare, reciprocating engine or turbine.

Removal of ammonia

Ammonia is an air pollutant and the cause of granular formation in exhaust gases when released into the atmosphere. Because ammonia dissolves in water, it is commonly found in waste water (eg, leachate) from landfills. Unlike gas from organic waste.

Known principles of ammonia removal can be used in the context of the concentrator and purifier of the environment described in this document. For example, wastewater containing ammonia can be treated with a substance (eg caustic or alkali such as sodium hydroxide or lime) that can raise the pH of the leachate. The filtrate with an elevated pH value can be fed to an aerator, where the ammonia contained in the wastewater will migrate into the aerator's exhaust air. The exhaust air of the aerator can be combined with combustion air and excess air used to operate the flare, piston engine or turbine providing heat for the concentration method.

In a flare, reciprocating engine, or turbine, ammonia supplied with the combustion air can significantly reduce the amount of another pollutant, oxides of nitrogen (NOx), that may be present in the combustion products. Such a reduction will be achieved by implementing a method known as selective non-catalytic reduction of MOH emissions. When ammonia enters the hot gas concentrator from the waste heat source, a reagent capable of converting ammonia into a stable salt (as in the removal of ZOx using alkaline cleaning agents) can be introduced into the method. For example, sulfuric acid can be fed into wastewater (eg, leachate) after discharge from the aerator. This acid can be used to separate ammonia as ammonium sulfate (MH4) 2504 when it is present in a concentrated liquid.

As shown in fig. 17, an alternative embodiment of a concentrator used to remove ammonia from landfill leachate may include a caustic or alkali underflow line 195 connected to a leachate underflow line 186. The combined caustic/leachate flow may be fed through an integrated aerator 201 before being fed to the concentrator unit 120. Aerator 201 can carry out the selection of gaseous ammonia, which is released into the absorbing gas with the help of pre-added acoustic or alkali. The captured gaseous ammonia may be fed back to the organic waste gas flare 130 or to the reciprocating engine or turbine via the ammonia feed line 194. As described above, ammonia in the flare 130, reciprocating engine, or turbine can significantly reduce MOH. Regardless, ammonia can be separated as a stable salt when reagent is added from reagent source 197 through reagent inlet 199 in concentrator 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 organic waste gas described herein includes combining heated gas and a pressurized wastewater stream to form a mixture, reducing the static pressure of the mixture to vaporize a portion of the liquid from the mixture to produce a partially vaporized mixture containing a concentrated liquid and liquid concentrate carried over, contacting the partially evaporated mixture with alkaline material to reduce the sulfur oxides content of the partially evaporated mixture, and removing some of the concentrated liquid carried over and the reduced amount of sulfur oxides from the partially evaporated mixture to produce liquid-free gas.

Another aspect of the method for removing sulfur from organic waste gas described herein involves recycling and combining the liquid waste stream with a liquid concentrate.

Another aspect of the organic waste gas desulfurization method described herein includes removing a portion of the carryover concentrate liquid and reduced sulfur oxides from the partially vaporized mixture and passing the partially vaporized mixture through a cross-flow gas scrubber to remove a portion of the concentrated liquid that transferred, and a reduced amount of sulfur oxides from the partially evaporated mixture.

In yet another aspect of the organic waste gas desulfurization method described herein, the partially vaporized mixture has a temperature of from about 66°C to about 88°C).

Another aspect of the method for removing sulfur from organic waste gas described herein involves the generation of exhaust gas during fuel combustion.

Another aspect of the organic waste gas desulfurization method described herein includes selecting a fuel from the group consisting of organic waste gas, natural gas, propane, and combinations thereof.

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

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

In yet another aspect of the organic waste gas desulfurization method described herein, the heated gas has a temperature of from about 482°C to about 649°C.

In another aspect of the method for removing sulfur from organic waste gas described herein, the wastewater contains from about wt. 96 to about 5 wt. 95 solids from the total mass of the filtrate.

In yet another aspect of the method for removing sulfur from organic waste gas described herein, the liquid concentrate is likely to contain at least about 1 wt. 95 solids from the total mass of the concentrate, more likely the liquid concentrate contains at least about 20 mass. 95 solids from the total mass of the concentrate, even more likely the liquid concentrate contains at least about ZOmass. 95 solids by weight of the concentrate, and even more likely the liquid concentrate contains at least about 5Omas. 95 solids from the mass of the concentrate.

In another aspect of the method for removing sulfur from organic waste gas described herein, the partially evaporated mixture contains from about 5 wt. 95 to about 20 wt. 95 liquid from the mass of the partially evaporated mixture, and it is more likely that the partially evaporated mixture contains from about 10 wt. 95 to about 15 wt. 95 liquid from the mass of partially evaporated mixture.

Another aspect of the organic waste gas desulfurization method described herein involves burning natural gas directly from a natural gas wellhead.

Another aspect of the method for removing sulfur from organic waste gas described herein includes selecting wastewater from the group consisting of leachate, return water, formation water, and combinations thereof.

Another aspect of the method for removing sulfur from organic waste gas described herein includes selecting an alkaline material from the group consisting of sodium hydroxide, calcium carbonate, and mixtures thereof.

Another aspect of the process for removing sulfur from organic waste gas described herein involves combining heated gas and a liquid wastewater stream containing alkaline material under pressure to form a mixture of them and to reduce the sulfur oxides content, reducing the static pressure of the mixture for evaporation a portion of the liquid from the mixture to obtain a partially vaporized mixture containing the concentrated liquid and liquid concentrate carried over, and removing a portion of the concentrated liquid carried over and the reduced amount of sulfur oxides from the partially vaporized mixture to obtain a liquid-free gas.

An aspect of the method for removing ammonia from a landfill leachate described herein includes combining a pH-increasing agent with a liquid wastewater stream to form a pH-enhanced wastewater stream, contacting the air stream with a pH-enhanced liquid wastewater stream under conditions, sufficient to remove ammonia from wastewater to produce an ammonia-enriched, high-pH, low-ammonia effluent stream, combining the heated gas with a high-pH, low-ammonia wastewater stream, under pressure to form a mixture, reducing static pressure of the mixture to evaporate a portion of the liquid from the mixture to obtain a partially vaporized mixture containing a concentrated liquid and a liquid concentrate carried over, and removing a portion of the concentrated liquid carried over and a reduced amount of sulfur oxides from the partially evaporated mixture to obtain a gas without content liquid

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

Another aspect of the method for removing ammonia from landfill leachate described herein involves the selection of caustic as a material to increase the pH value.

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

Another aspect of the wastewater concentration method according to the disclosure of the present invention includes the combination of heated gas and liquid wastewater within the hermetic section of the channel to form a mixture that flows through the hermetic channel under the influence of the discharge created by the exhaust fan located after the hermetic channel, the supply of the flowing mixture through a section of the channel with a limited cross-sectional area compared to the cross-sectional area where the mixture is created, thereby increasing the flow rate and creating turbulence, which leads to the appearance of transverse forces between the continuous gas phase and the surfaces of the limited channel opening in contact with the discrete liquid phase , which breaks the drops and other geometric shapes of the flowing liquid into very small drops, thus creating a long boundary surface between the flowing gas and liquid wastewater, which ensures a rapid approach to the adiabatic saturation temperature of the liquid-gas mixture as a result of the quickly transferred of heat and mass from gas to liquid and from liquid to gas, respectively, to obtain a partially vaporized mixture containing a concentrated liquid and a liquid concentrate carried over, and removing part of the concentrated liquid carried over from the vaporized mixture to obtain a gas without water content.

Although certain embodiments and details presented have been shown to illustrate the invention, it will be understood by those skilled in the art that various changes in the methods and apparatus disclosed herein may be made without departing from the scope of the invention.

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