RU2060430C1 - Plant for thermal decontamination of liquid waste - Google Patents

Abstract

FIELD: flame method of liquid waste decontamination. SUBSTANCE: plant has vertical firebox with burner unit, injectors for feeding liquid waste, tap hole for melt discharge, gas vent holes, annular bubbling evaporator mounted coaxially in respect to firebox and divided by partition into sections communicating with outlet holes of firebox, heat exchanger with inlet and outlet chambers. Heat exchanger outlet chamber communicates via piping with air blower and ozone source. Outlet ends of heat exchanger tubes are arranged below emergency drain pipe. Outlet gas duct carrying steam-gas mixture accommodates mixer joined through piping with air blower and ozone source. EFFECT: improved design, enlarged functional capabilities. 2 cl, 1 dwg

Description

 The invention relates to devices for thermal disposal of liquid waste and can be used in various industries where liquid waste is generated, which must be neutralized by fire.

 A known installation for thermal disposal of liquid waste containing a vertical fire chamber with a burner, nozzles for supplying waste water, a tap hole for outputting melt, an annular evaporator mounted coaxially to the fire chamber and divided by partitions into sections, each of which is connected by a gas duct to the fire chamber. Fuel and air are supplied to the fire chamber through a burner. There, through the nozzles, concentrated mineralized effluents from the annular evaporator are injected through the nozzle. Hot products of fuel combustion in the fire chamber are divided into two streams: one stream, passing the treatment zone of mineralized concentrated effluents, provides optimal conditions for their treatment, the second stream enters the treatment zone of the evaporation with organic matter. Mineralized wastewater treatment products enter the evaporator section. When they are bubbling through a layer of effluents, distillation of boiling organics, evaporation of effluents and purification from mineral impurities occur. The flue vapor enters the fire chamber, which is connected to the heat exchanger. Organic-free vapor is discharged from the process through a valve. The distribution of the flows of hot products of fuel combustion is carried out by changing the flows in the evaporator.

 A disadvantage of the known installation is the increased fuel consumption for the neutralization process associated with the re-heating of the combustion products, which is the evaporation, to the reaction temperature.

 Closest to the technical nature of the claimed solution is the installation for the neutralization of waste stocks containing a vertical fire chamber with a burner, nozzles for supplying waste water, a tap outlet for fusion and gas outlet openings, a bubbler type annular evaporator mounted coaxially to the fire chamber, divided by partitions into sections connected to the outlet openings of the fire chamber by gas flues, a heat exchanger located above the bubbler evaporator and connected to the fire chamber a flue at the location of the gas burner device. Fuel and air are supplied to the fire chamber through a burner device, then concentrated mineralized effluents from the evaporator section are pumped through the wastewater nozzles. Hot products of fuel combustion in the fire chamber are divided into two streams. One stream, passing through the treatment zone of mineralized concentrated effluents, provides optimal conditions for their treatment, enters the evaporator section, the second stream through the hole enters the gas duct, where it transfers heat through the surface of the pipes to air or gas emissions and is released into the atmosphere. Air or gas emissions enter the inlet chamber, from where they are bubbled through pipes, the ends of which are below the level of the source effluents, through the effluent layer and through the pipes enter the outlet chamber, from where they are supplied to the upper part of the fire chamber through an additional gas duct through a gas burner device. Passing through the pipes, the air receives heat from the hot products of combustion in the duct. This heat is partially used to heat the initial effluents, remove boiling organic matter and partially to heat the air and organic matter before entering the combustion zone. The initial effluent enters the bubbler evaporator, sections pass in which the air heated in the heat exchanger is bubbled. In this case, the initial effluents are heated, boiling organics are distilled off. A mixture of air and low boiling organics passes through the pipes and enters the outlet box of the heat exchanger, from where it enters the fire chamber through the burner through an additional gas duct. Primary treated effluents enter the evaporator section. When bubbling through a layer of effluents, evaporation of effluents and gas purification from mineral entrainment occur. A gas outlet is located between the burner and the wastewater nozzles. The distribution of hot fuel combustion products is carried out by changing the level in the evaporator section.

 The disadvantage of this installation is the increased fuel consumption for the neutralization process, associated with the heat consumption of the hot combustion products for heating the air in a heat exchanger acting as an air heater. Given the insignificant heat transfer coefficient of the air heater and the need for maximum use of the heat of the combustion products, the latter will lead to an increase in heat exchange surfaces and, as a result, to a significant consumption of metal and installation dimensions.

 Thus, a significant drawback of the above installations is that during the neutralization of wastewater containing organic impurities, which form azeotropic or inseparable boiling mixtures with water, which during the vaporization process will be released with the gas-vapor mixture into the atmosphere, polluting it, which will require additional devices for their neutralization, additional fuel consumption for the neutralization process and will lead to a decrease in the efficiency of the installation.

 The purpose of the invention is the creation of a plant for the thermal neutralization of liquid waste, the use of which will eliminate the ingress of harmful organic impurities into the atmosphere, abandon additional devices for their neutralization and thereby reduce fuel consumption.

 This goal is achieved in that the installation contains a vertical fire chamber with a burner, nozzles for supplying liquid waste, a tap hole for outputting melt, outlet openings for the exit of gases, a bubble-type annular evaporator mounted coaxially to the fire chamber, divided by partitions into sections connected to the outlet openings of the fire chamber, heat exchanger with inlet and outlet chambers. The inlet chamber of the heat exchanger is connected by a pipe to the blower and a source of ozone supply, while the outlet ends of the tubes of the heat exchanger are located below the emergency drain pipe. In the outlet gas duct of the vapor-gas mixture behind the annular bubbler evaporator, a mixer is installed, which is connected by a pipe to the blower and a source of ozone supply.

 A comparative analysis of the invention with the prototype allows us to conclude that the invention is new in that the inlet chamber of the heat exchanger is connected by a pipe to the blower and an ozone supply source, while the outlet ends of the tubes of the heat exchanger are located below the emergency drain pipe. In the outlet gas duct of the vapor-gas mixture behind the annular bubbler evaporator, a mixer is installed, connected by a pipeline to the blower and a source of ozone supply. These features ensure the invention meets the criterion of "novelty."

 Comparison of the claimed solution, not only with the prototype, but also with other technical solutions in the art allow us to conclude that it meets the criterion of "inventive step".

 The drawing shows a diagram of the proposed installation.

 The installation consists of a vertical firing chamber 1 with a burner 2, nozzles 3 of liquid waste and letka 4 for withdrawal of melt. The fire chamber 1 is provided with outlet openings 5. An annular bubbler evaporator 6 is mounted coaxially to the fire chamber 1 and is connected to the outlet gas duct 7 of the vapor-gas mixture. Above the annular bubbler evaporator 6, a heat exchanger 8 is placed, including an inlet 9 and an outlet 10 of the chamber, heat exchange tubes 11 with tube plates 12 and 13, a shell 14, and an emergency discharge pipe 15. The inlet chamber 9 of the heat exchanger 8 is connected by a pipe 16 to the blower 17 and an ozone supply source 18. The output ends of the pipes 11 of the heat exchanger 8 are located below the emergency discharge pipe 15. The outlet chamber 10 of the heat exchanger 8 is connected through a gas burner 2 to the firing chamber 1 by an additional gas duct 19. A mixer 20 is installed in the outlet gas duct 7 of the gas-vapor mixture, connected by a pipe 16 to the blower 17 and an ozone supply source. In the outlet chamber 10 of the heat exchanger 8 there is a nozzle 21 for supplying liquid waste, and a nozzle 22 is installed in the annular bubble evaporator 6, connected by a pipe 23 to nozzles 3 for supplying liquid concentrated waste.

 Installation works as follows.

 The fuel is fed into the fire chamber 1 through the burner 2. The combustion air before being fed into the gas burner 2 (the supply is carried out from conditions ensuring the complete absence of chemical underburning) from the blower 17 is saturated with ozone from the source 18. The ozone-air mixture through pipeline 16 enters the inlet chamber 9 of the heat exchanger 8, formed by pipes 11, pipe boards 12 and 13, the shell 14. Through the pipes 11, the ozone-air mixture enters the outlet chamber 10, where liquid waste contaminated by time passes through the pipe 21 organic and mineral impurities. In this case, liquid waste is bubbled by placing the emergency discharge pipe 15 below the outlet ends of the pipes 11 of the heat exchanger 8. The liquid waste treatment products from the outlet chamber 10 of the heat exchanger 8 are sent through an additional gas duct 19 to the gas burner device 2, where they are burned together with the fuel. The supply of ozone from the source 18 is carried out from conditions that ensure the oxidation of harmful organic impurities contained in liquid waste.

C=C

__→

C

C

-R-

+R′-

+R″′+

O₂
Вредные органические вещества, содержащиеся в жидких отходах и имеющие связь

C=C

реагируют с озоном следующим образом:

+O₃

-C⁺-OO^-+O C

__→

биполярный ион озонид
Предварительно обработанные озоновоздушной смесью жидкие отходы (в качестве устройств для получения озона могут быть использованы озонаторы типа ПО-3) в теплообменнике 8 через патрубок 15 аварийного слива поступают в кольцевой барботажный испаритель 6, соединенный через выходные отверстия 5 с огневой камерой 1.The connection of the inlet chamber 9 of the heat exchanger 8 with a pipe 16 with a blower 17 and an ozone supply source 18 allows you to efficiently process organic, odorous, mineral and other impurities in liquid waste. In this case, there is a direct decomposition of organic substances with the participation of one oxygen atom, the addition of a whole ozone molecule to an oxidizable substance with the formation of ozonides, a catalytic increase in the oxidizing effect of oxygen in ozonized air. During ozonolysis, ozone is fixed on a double or triple carbon bond with its subsequent rupture and the formation of ozonides, which, like ozone, are unstable compounds and quickly decompose:

C = c

__ →

C

C

-R-

+ R′-

+ R ″ ′ +

O ₂
Harmful organic substances in liquid waste and associated

C = c

react with ozone as follows:

+ O ₃

-C ⁺ -OO ^- + OC

__ →

bipolar ion ozonide
Liquid waste pre-treated with an ozone-air mixture (PO-3 type ozonizers can be used as ozone production devices) in a heat exchanger 8 through an emergency discharge pipe 15 enter a ring bubbler 6 connected through outlet openings 5 to a fire chamber 1.

 In the annular bubbler evaporator 6, due to the heat from the combustion of fuel, liquid waste is evaporated to the required concentrations of mineral impurities, followed by processing of the concentrate by pumping it through a pipe 23 through nozzles 3 into the fire chamber 1, which maintains the required temperature level. In the fire chamber 1, trapping of mineral impurities takes place, followed by their removal through the notch 4 in the form of melt. The uncaught part of mineral impurities together with the vapor-gas mixture enters the annular bubbler evaporator 6, where it is cleaned of mineral entrainment and then enters the outlet gas duct 7, in which the mixer 20 is connected to the ozone supply source 18.

 When evaporating liquid wastes containing harmful organic impurities that form azeotropic or inseparable boiling mixtures with water, characterized by a minimum boiling point (ethyl alcohol, acetonitrite, butyric acid), significantly lower than the boiling point of water. The latter in the process of sparging with hot flue gases in an annular evaporator 6 will be distilled off with the vapor-gas mixture into the atmosphere, which will lead to environmental pollution and will require additional devices and installations for their neutralization.

 However, the treatment of a gas-vapor mixture with an ozone-air mixture by placing a mixer 20 in the outlet gas duct 7 connected by a pipeline 16 to an ozone supply source 18 completely eliminates the ingress of harmful organic substances into the environment and does not require additional devices and installations for their neutralization, which ultimately increases the efficiency installation work as a whole.

 Using the proposed installation in comparison with the prototype will eliminate the ingress of harmful organic impurities into the atmosphere due to the preliminary and subsequent treatment of liquid waste and gas-vapor mixture with an ozone-air mixture, abandon additional devices and installations for the disposal of harmful organic impurities in the exhaust gas-vapor mixture, and reduce specific fuel consumption by the process of neutralization due to the full use of heat from the treatment of concentrated liquid waste in a ring bubbler and vaporizer, to provide optimal conditions for the neutralization of liquid waste with a variable composition, while maximally catching mineral mixtures within the installation, which can be reused for technological purposes.

Claims (2)

 1. Installation for thermal disposal of liquid waste containing a vertical fire chamber with a burner, nozzles for supplying waste, a tap hole for outputting melt, gas outlet openings, a bubble-type annular evaporator mounted coaxially with the fire chamber, divided by partitions into sections connected with fire chamber outlet openings, a heat exchanger with inlet and outlet chambers, characterized in that the inlet chamber of the heat exchanger is connected by a pipe to the blower and a source ohm of ozone supply, while the output ends of the pipes of the heat exchanger are located below the emergency drain pipe.  2. Installation according to claim 1, characterized in that in the outlet gas duct of the vapor-gas mixture behind the annular bubbler evaporator, a mixer is installed, connected by a pipe to the blower and a source of ozone supply.

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