JPH03295569A - Method and apparatus for separaiting and treating organic waste - Google Patents

Abstract

PURPOSE: To remove polynuclear aromatic structures as byproducts by mixing a reducing agent in organic wastes for direct chemical reduction of the wastes, then reducing the wastes at temperatures of 600 deg.C and higher in a first region, and cooling and enriching the first part of the gasified components obtained. CONSTITUTION: Wastes are passed through a preheater 100, are guided into a reduction container 104, are mixed with a gasified reducing agent H(2 ) through a waste/reducing agent inlet 106, and are heated by an incandescent bar 112, and the gasified wastes reduced are passed through a retention area 116, water is atomized and injected, and molten halogenated hydrogen gas is enriched in a tank 118 and recovered. Next, an acid neutralizer is added from a neutralizer supply means 120 to neutralize the gas. Unenriched gas containing the reduction product and steam is coated and enriched by passing it through a cooling region 125. Further, gas left unenriched is passed through a demister 130 and a collecting frame 132, an oxidizer is injected, an oxidation region 136 is heated to promote oxidation, and the final product is released through a chimney 138.

Description

Detailed description of the invention [Industrial field of application] The present invention relates to a system for the decomposition of organic waste, in particular a method for the decomposition treatment of organic waste with or without polyhalogenated waste, and a method for carrying out the method. It relates to a device for.

[Prior Art] It is known to decompose halogenated organic wastes by reduction treatment using, for example, sodium napthalide or sodium metal. It is also known to decompose halogenated organic wastes by oxidation, for example using high temperature incineration. These known methods have the limitation or drawback that they can only be used for certain types of waste. Furthermore, the chemicals for decomposition are often dangerous to handle, and decomposition can lead to the formation of highly toxic by-products.

Environment Canada Economics and Technical
Review Report E.P. Niss 3-EC-83
-1 comments.

Considering the doubts regarding the carcinogenicity of PCBs and the fact that they do not degrade in nature over extremely long periods of time,
14. Actually used in transformers and capacitors.
PCB amount of 8x lo”Kg (No. 7 of said report)
The table below shows how big the problem is.

[Problem to be Solved by the Invention] Furthermore, waste is accumulating in many areas far removed from existing large-scale incinerators available in the United States and Canada for waste incineration, and such problems cannot be solved. Its essence is deep-rooted. Additionally, the public is aware of the potential dangers of PCBs to public health, which may also prevent the transport of PCBs to existing facilities.
Things are getting complicated. The occurrence of published PCB emissions will further exacerbate these types of problems.

The current method of disposing of this type of material is by incineration in large-scale facilities. While there is a requirement for this method to achieve very high percentiles of effectiveness for disposal, there is concern that the report may demonstrate that disposal remains ineffective for long periods of time. There is. In addition, highly toxic by-products such as chlorinated dioxins are obtained when incineration or oxidation is performed at conditions outside the precise optimum temperature and residence time.

Referring to page 28 of the above-mentioned report, PCB
A problem that has been identified as contributing to incinerator collapse is the formation of a ring of "agglomerate" during incineration. This type of [glop J formation is an inherent by-product of incineration systems and likely represents a partial recombination of molecules into ring compounds. This is one of the reasons for proposing an improved method.

Degradation of solid and liquid organic wastes of hydrocarbons, thermal destruction or thermal decomposition due to lack of air is suppressed when tars and polynuclear aromatic hydrocarbons with 1 to 5 aromatic rings are formed. It had been.

In view of the above-mentioned points, the present invention provides for removing polynuclear aromatic structures contained in organic waste as a by-product of a predetermined reaction by removing the resulting molecules in gaseous form at a concentration sufficient to saturate or reduce them. It is an object of the present invention to provide a method for decomposing and treating organic waste by adding a reducing agent such as hydrogen.

Another object of the invention is to provide an apparatus for the reduction and subsequent oxidation of organic wastes.

[Means for Solving the Problems] The - aspect of the present invention comprises reducing organic waste in the presence of a gaseous reducing agent and then cooling it in the presence of water to obtain a concentrated liquid;
While most of this concentrated liquid is recovered and used for further processing,
The present invention provides a method for treating organic waste, in which a portion of the waste is reused in the cooling treatment described above.

Another aspect of the invention is a method of decomposing organic waste that combines gas-phase chemical reduction at elevated temperatures in a reducing atmosphere and oxidation of the thermal reaction mixture of this chemical reduction in a high-temperature incinerator. .

In the present invention, it is also possible to perform a plurality of reduction treatments on waste and then recover the reduction products.

Additionally, in the present invention, it is advantageous to preheat the waste if the waste is previously reduced before being injected into the separate reduction zone.

In the present invention, it is also possible to collect the energy dissipated during the collection process by heat exchange, and use this collected energy to preheat the uncollected material to be oxidized in the subsequent process.

Furthermore, other aspects of the invention provide that within a separate preheating area,
An apparatus for decomposing organic waste is provided with preheating means having an oxygen/fuel burner for preheating the waste before injection into the reduction zone.

In the present invention, it is possible to capture the energy dissipated during the oxidation process by heat exchange and to transfer this captured energy to the waste to preheat the waste before the reduction treatment.

Another aspect of the present invention is to apply a chemical reduction treatment to organic waste using a gaseous reducing agent at a temperature of about 60Q°C or higher, and to apply a gaseous oxidizing agent to the resulting thermal reaction mixture at a temperature of about 1000°C or higher. A method for decomposing organic waste that uses oxidation treatment.

Additionally, other embodiments of the invention provide organic waste at a temperature of about 700°C.
A reduction treatment using a gaseous reducing agent is performed at a temperature range of from about 900°C to a residence time of about 0.1 to about 10 seconds, and the resulting thermal reaction mixture is then subjected to a reduction treatment using a gaseous reducing agent at a temperature range of from about 7000°C to about 1400°C. Oxidation treatment using a gaseous oxidizing agent of about 1 to about 4 mm
A method for decomposing organic waste with a residence time of seconds.

In the present invention, organic wastes, e.g. halogenated organic wastes, in the form of finely divided slurries such as liquids, pumped sludges, contaminated sediment/water mixtures or ground solids, e.g. halogenated organic wastes, are placed in a pressurized reaction vessel in the absence of oxygen. It can be conveniently carried out by direct upward injection. In this case, the reaction vessel is heated to a temperature of about 600°C or higher, preferably about 7°C.
Maintain a temperature range of 00°C to about 900°C.

In another embodiment of the present invention, a reduction treatment container whose horizontal cross-sectional shape is approximately circular is used. This container has a ceramic tube arranged at its center and an outlet of the reducing container arranged above the opening of the ceramic duplex.

The waste and gaseous reducing agent are mixed well at the upper edge of the container and poured into the container. When injected in this manner, a baffle plate effect is obtained. Once the gaseous waste is injected into the top of the container, it passes through the hole in the tube and then upwardly through the tube and its opening to the bottom of the container and from there to the next area. Sent. A reduction vessel having a tube and an upper inlet as part of its construction allows for greater travel distance of the gaseous waste within the vessel and greater area of the interior surface of the vessel that is accessible to the gaseous waste. be. The organic substances contained in the solid waste can be evaporated when the solid waste boils as it hits the hot container surface. In such embodiments, a water stream is routed through the bottom of the container to remove the specific substance, with the removed specific substance being carried by the water stream to a collection tank. A steady stream of gaseous reducing agent passes through the lower region of the vessel above the water stream to avoid contact of the gaseous waste with the water stream.

The waste can be injected with a gaseous reducing agent such as hydrogen, gaseous ammonia, natural gas, methane, propane, steam or mixtures thereof. The reduction is carried out with or without the addition of metal catalysts such as iron, zinc, tin or nickel in the form of iron scrap, powdered zinc, powdered tin, powdered nickel which can be injected into the vessel to accelerate the reduction reaction. <Can be implemented.

However, in a preferred embodiment, the waste is continuously injected with hydrogen into a preheated reduction vessel and the reduction vessel is heated from above atmospheric pressure to 1 atm above ambient pressure without the addition of catalyst. It has a process of maintaining it with internal pressure.

In a preferred embodiment, the waste to be injected into the reduction vessel is also preheated.

The residence time of the gaseous substance in the reaction container is about 0.1 seconds or more,
The reaction vessel can be positioned and the injection rate can be adjusted, preferably from about 5 seconds to about 10 seconds. A particularly effective residence time to effectively complete the reduction is about 5 seconds.

The reduction is carried out at a temperature of about 600°C to about 1100°C, preferably about 7
00℃ to about 900℃, especially about saa℃ to about 9 (to
It can be carried out in the temperature range of °C.

The reduction can also be carried out in the presence of metal catalysts such as iron, nickel, zinc or tin. This catalyst is iron scrap,
It can be in the form of powdered nickel, powdered zinc or powdered tin.

Organic waste includes organic compounds such as halogenated biphenyls, halogenated benzenes, halogenated phenols, halogenated cycloalkanes, halogenated alkanes, halogenated alkenes, halogenated dioxins and halogenated dibenzofurans. It may or may not contain. For example, organic waste contains chlorinated biphenyls, also known as polychlorinated biphenyls (PCBs), chlorinated benzenes, chlorinated phenols, chlorinated cycloalkanes, chlorinated alkanes, chlorinated dioxins, and chlorinated organic compounds. There are cases where

The organic waste can be in the form of liquids, pumped sludges, finely particulate slurries such as contaminated sediment/water mixtures, crushed or shredded solids such as contaminated wood waste or soil. Such wastes include, for example, polychlorinated biphenyls (PCBs), which are waste products from capacitor and transformer manufacturing processes or obsolete electrical or non-electrical equipment.
) containing products such as oils and lubricants.

Additionally, organic waste may contain non-halogenated organic compounds. This can be, for example, shredded or granular organic solids, such as shredded pathogenic waste.

The reaction vessel for the reduction stage of the process of the invention is lined with a chemically and heat resistant material suitable to withstand the gaseous by-products generated, eg hydrogen halides such as hydrogen chloride. The cleaning auger is also filled to remove solid waste or by-products such as metals, metal salts, silicates or other solids that may accumulate within the vessel.

Gaseous reducing agents such as ammonia gas are hydrogen.

Although lower in cost and potentially less explosive than methane or propane, the latter reducing agent offers certain advantages. However, although the use of hydrogen gas is preferred for many reasons, propane may be used if the Br3 content of the waste is potentially low enough to cause adequate oxidation.

However, the use of a reducing vessel and the selection of hydrogen gas as the reducing agent have many advantages and are optimal.

Other aspects of the invention include the required dimensions of the reduction vessel to carry out continuous treatment by utilizing hydrogen and the production of carbon in the case of a road mobile system for on-site decomposition of accumulated PCBs and halogenated wastes. possibility can be minimized. Decomposition of PCBs, i.e. hazardous waste, into gaseous fuels can reduce the need for additional fuel and the amount of additional combustion air required for the fuel, thereby reducing the size of the secondary incinerator and overall decomposition equipment. be able to.

Safety requirements for the reduction vessel include multiple purges with an inert gas such as nitrogen to ensure the absence of oxygen (eg, air) within the vessel and eliminate the possibility of explosion.

Since this method is generally a continuous method, it is possible to easily obtain an anoxic state by repeating purging.

In a preferred embodiment, the reduction vessel is connected directly to the combustor and both vessels are purged first.

In operating a reduction vessel directly adjacent to, and preferably directly connected to, a high temperature oxidation zone (combustor), the reduction zone is maintained at a sufficiently higher pressure than within the combustor to direct air from the combustor to the reduction vessel. It is desirable to prevent backflow of oxidizing agents containing oxidants. Furthermore, the array of reduction zones has mixing nozzles in which the pressurized reducing gas is bombarded at high speed at a low level location within the zone and a gas retention zone containing the reduced gas product located above it. It mixes intimately with the incoming waste and is sprayed to separate the reducing zone from the oxidizing zone at its outlet. A ceramic taishōme can be provided at this interface region between reduction and oxidation to prevent flashback.

Thermal reducing gas is introduced into the oxidation zone via the combustion mantle, combustion nozzle or suitable means for proper mixing with the combustion air introduced into the oxidation zone so that the flame end is optimally located within the oxidation chamber. do.

Another advantage of using normally gaseous hydrogen is that it uses a jet stream of hydrogen to collide with the substance to be reduced, reducing the mixing ratio.
There is therefore the possibility of achieving a highly active mixing zone that utilizes the as-supplied hydrogen to optimize the reduction process.

in the case of fluid waste, colliding the waste jet with a lateral jet of hydrogen to achieve atomization by intimate mixing;
The chemical effectiveness of the reduction process can be promoted.

In one example, a CALDYN™ type radially internal gas cross nozzle is used.

This system can handle fluid waste containing trains up to 1/4 inch mesh size and droplets as small as 40 microns can be obtained economically.

Further, the reduction can also be carried out in the presence of water vapor that does not suppress the reduction reaction. It is thus possible to decompose organic wastes, sludges or sediments which contain significant amounts of water, for example contaminated port sludges or sediments.

The thermal reaction mixture from this reduction process is generally dehalogenated, halogenated or reduced hydrocarbons or nearly dehalogenated hydrocarbons, including hydrogen halides such as hydrogen chloride, water and excess hydrogen. contains.

In a preferred embodiment, the reaction vessel to be used for the reduction adjoins vertically a second vessel to be used for the second oxidation phase.

About 600℃ to about 1000℃, especially about 800℃ to about 9
The thermal reaction mixture from the reduction step carried out at a temperature of 00 °C,
The continuous expansion of the gases as reductive destruction occurs, together with thermal convection and the resulting pressure as a result of evaporation and volatilization of the injected liquid or partially liquid waste, can cause simple insulating ceramic or refractory lined pipes to You can push through.

Excess air or oxygen is transferred to the second vessel to heat the reaction mixture in a turbulent flow of hot gases until the complete combustion of these gases occurs at approximately 1000°C.
It can be introduced in such a way that it occurs with oxygen promoting at temperatures above. Useful temperatures range from about 1000°C to about 1500°C, particularly from about 1200°C to about 1400°C.
is within the range of

The dimensions of the second oxidation vessel are such that the residence time of the thermal reaction mixture within the combustion chamber is from about 1 second to about 4 seconds, preferably about 2 seconds or more. Additionally, the combustion chamber of the second vessel can be lined with a material that can withstand hot acid gases, such as hydrogen chloride, passing through the chamber. The heat release from this second vessel is quickly cooled and scrubbed with water and an aqueous alkali such as sodium hydroxide mist or sodium carbonate to remove and neutralize acid gases.

Depending on the waste, it may be desirable to recover some of the initial reduction products.

In a second aspect of the invention, the product in the reduction step is cooled in the presence of a water mist injected into the gaseous reduction product flow path. The gaseous residue is then further cooled and a second
The substance, which remains a gas even after undergoing this concentration process, is collected on the oxidized surface.

If the waste starting material contains halogenated organic material, the initial reduction product is hydrogen halide gas.

If this gas is initially dissolved in the collected acidic liquid, most of it is separated. This acidic liquid is neutralized in the presence of a base or other basic substance such as sodium bicarbonate, calcium carbonate, sodium hydroxide.

Depending on the starting materials and the operating conditions of the process, a second liquefied portion having a lower liquefaction temperature than the first liquid portion can then be collected. For example, if the starting material contains a large amount of chlorobenzene, a second liquid containing a large amount of organic material containing the reduction product benzene can be collected. In this example, the bulk of the second liquid contains water that was not collected as part of the first liquid. If the water content in the second liquid forms a separation layer from the organic material described above, it can be separated, removed and recycled for use as a water mist in the initial cooling step for the product in the reduction step. You may use it.

Gaseous substances remaining after the second cooling step can be transferred to the oxidation zone. It is desirable to preheat the oxidizing material before subjecting it to suitable oxidizing conditions. The heat exchange step in the actual embodiment is used to capture and transfer the energy dissipated or rejected during the second cooling step to facilitate preheating of the material to be oxidized. Such a heat exchange step can be performed alone for the heating step before the oxidation step.

A de-misting step can be performed before the pre-heating step to ensure that all condensate material is removed from the residual gaseous material. The heat exchange step in the actual embodiment is used to transfer the energy liberated during the oxidation step to the waste preheating step before reduction.

This transfer of energy is preferably accomplished by heating water to obtain steam within a closed area. Hot water or steam is circulated in a closed area from the oxidation zone to the waste sub-hot water zone and is again used to preheat the waste.

As mentioned above, it is usually preferred to inject the reducing agent and waste through a nozzle so that they are intimately mixed.

If a situation arises in which it is inconvenient to inject the waste through the nozzle, the waste can first be injected into the melted waste before introducing the waste into the reduction chamber. An example of a material used to melt incinerator ash is fused silica. In such a preferred embodiment of the invention, the waste to be reduced is evaporated from the melted material and then reduced using a gaseous reducing agent which is injected separately from and before the melted material.

[Experimental Examples] The present invention will be explained below using experimental examples, but the present invention is not limited to these experimental examples.

Experimental Example 1 1 molar equivalent of polychlorinated biphenyl (^rochlor
1248 (trade name) was reacted with 22 molar equivalents of hydrogen in a first reaction chamber at a temperature of 875°C and 1 atm pressure gauge for a reaction time of about 30 seconds. This reaction resulted in 99.9% decomposition and the resulting gaseous reaction mixture contained hydrogen chloride, benzene,
Contained biphenyl and chlorobenzene. Next,
This gaseous reaction mixture was passed through an intermediate tube to a second tube at 875°C.
The mixture was passed through a reaction chamber where oxidation was carried out. A 5% excess of preheated air was mixed with the gaseous reaction mixture in the second reaction chamber and the oxidation was completed at a temperature of 1000-1200<0>C with a residence time of 2 seconds. This oxidation of the gaseous reaction mixture was effective to complete the oxidation of the reactants remaining within the mixture.

Experimental Example 2 9 molar equivalents of monochlorobenzene and 2 molar equivalents of 1.
2.4-) dichlorobenzene in the first reaction chamber at 925
It was reacted with 21 molar equivalents of hydrogen at a temperature of 0.degree. C. and 1 atm pressure with a reaction time of 30 seconds. This reaction resulted in 99.95% dehalogenation of chlorobenzenes. The gaseous reaction mixture was then passed at 875° C. via an intermediate tube into a second reaction chamber where the oxidation took place.

A 5% excess of preheated air was mixed with the gaseous reaction mixture in the second reaction chamber and the oxidation was completed at a temperature of 1000-1200<0>C with a residence time of 2 seconds. This oxidation of the gaseous reaction mixture was effective to complete the oxidation of the reactants remaining within the mixture.

Experimental Example 3 1 mol of chloroform was reacted with In mol equivalent of water vapor in the first reaction chamber at 950°C and 1 atm for a reaction time of 30 seconds. This reaction resulted in 99.9% dehalogenation of chloroform. The gaseous reaction mixture was then heated to 875
℃ through an intermediate tube to a second reaction chamber where the oxidation took place. A 5% excess of preheated air was mixed with the gaseous reaction mixture in the second reaction chamber and the oxidation was completed at a temperature of 1000-1200<0>C with a residence time of 2 seconds. This oxidation of the gaseous reaction mixture was effective to complete the oxidation of residual reactants within the mixture.

Experimental Example 4 A hexane solution of 0.44% hexachlorobenzene was mixed with hexane at a flow rate of 1.8 mmol per minute and hydrogen at a flow rate of 17 mmol per minute.
Water was passed through the tubular reaction chamber for 60 minutes at a flow rate of 28 mmol per minute. The reaction temperature at the injection end of the reaction chamber is 1000°C, and the reaction temperature at the middle part is 950°C.
The outlet temperature was set at 900°C.

The average residence time was 3.3 seconds. The reaction product was collected in a concentration flask at the outlet of the reaction tube connected to the XAD7 resin cartridge. When the contents of the flask and test tube were analyzed for hexachlorobenzene and chlorobenzene, the decomposition removal rate of hexachlorobenzene and gold-chlorobenzenes was 99.999.
%Met. The reaction products were methane, hydrogen chloride, benzene, and chlorobenzenes. And, as chlorobenzenes, 1,2,3,4-tetrachlorobenzene,
Pentachlorobenzene and hexachlorobenzene were detected. According to other tests, chlorobenzenes include monochlorobenzene, 1.2-dichlorobenzene, 1.3
-dichlorobenzene, 1.4-dichlorobenzene, 1.
2.3-) dichlorobenzene, 1.2.4-) dichlorobenzene, 1,3.5-trichlorobenzene, 1,2
, 3,5-tetrachlorobenzene and 1,2,4.5
-Tetrachlorobenzene was detected. Approximately the same amount of water was recovered from the product in each reaction as was injected.

The experimental examples described above constitute laboratory tests to establish efficacy and residence time.

In carrying out the present invention at an effective production level, it is necessary to properly preheat the reduction chamber to the reaction maintenance temperature.

Considering the advantages offered by the use of hydrogen and the mandatory need to provide an effective gas barge as mentioned above, the preheating of the vessel in question is based on electrically heated preheating elements as opposed to active heating methods such as gas combustion. It is preferable to use passive heating means such as

Due to the highly active chemicals typically produced by this process, the use of protective, chemical resistant container linings is important. This requirement is not contradictory to the use of radiant heat.

Steam or superheated steam is used as a purge gas or preheating agent.

In FIG. 1, a reduction vessel 10 for carrying out the method is shown.
has a metal shell 12, which is nearly independent, on which a combustion chamber 14 is mounted.

The reduction vessel 10 has one or more inlet nozzles (see FIG. 2) for injecting the waste containing ground solids.
and the liquid portion of the waste is atomized by a jet stream of hydrogen gas through the ring of nozzle 27.

The vessel 10 also includes a bank of known commercially available types of radiant electric heaters, such as interior wall lined carborundum silicon carbide Grover heaters.

Chemical resistant fiber flux (FIBERFRAX,
A ceramic insulator 24 protects the shell 12 while ensuring a safe processing thermal environment locally in the container 10.

The bottom 26 of the shell 12 has an auger 28 and a sealed outlet 30 to allow for washing away solid inorganic residues.

A passage 32 connects the vessel 10 and the combustion chamber 14 for upward passage of the gaseous reduction products. To ensure a safe positive pressure differential between reduction vessel 10 and combustion chamber 14, passageway 32 is located and dimensioned to control the pressure within vessel 10. A blowout panel (not shown) protects the vessel IO from overpressure explosions.

The combination of the air supply nozzle and the combustion grid ensures safe and stable combustion within the combustion chamber 14.

In FIG. 2, each nozzle 20 positioned as shown in FIG. 1 has a liquid population 21 and a gas population 23. In FIG. The gas population 23 is controlled by the control valves 201 and 203.
are connected to pressurized nitrogen and pressurized hydrogen sources (not shown) corresponding to the inlets, so that both vessels 10/
14 is purged and then subjected to chemical reduction treatment.

The exhaust port 36 of the combustion chamber 14 is connected to an acid gas scrubber and a centrifugal fan or particulate removal device 61, taking into account in particular the hydrogen chloride content of the exhaust gases.

FIG. 3 diagrammatically shows a decomposition device 40 with a reduction chamber 10 supporting a combustion chamber 14. In FIG. Control valve 5 supplying liquid waste or liquid source such as PCBs or PCB-containing sludge
0 to the inlet 21 of the nozzle 20 in the chamber 10.

The reduced gases are passed through passage 32 to combustion chamber 14 . Variable air population control member 54 can be adjusted to operate combustion chamber 14 at approximately atmospheric pressure.

passing the exhaust gases from the passage 56 to a scrubber system 60, a centrifugal fan particulate removal device 61 and a cooling shower 62;
It is then released into the atmosphere through the chimney 65.

The system includes a neutralized water tank 67, a cooling water tank 69, and associated pumps and control members.

This overall system does not exclude other types of scrubbers.

FIG. 4 shows a low floor trailer 9 with hydraulic actuators 92 for positioning the complex reduction/combustion vessel 10/14.
1 is a conceptual diagram of a practical device such as 0.

Steam from the steam generator may be utilized as a purge material for the combination vessel 10/14 and as a preheat material for the reduction combustion chamber 10/14.

Process control instruments located within the auxiliary trailer 95 provide automatic control and backup through instruments and control members (not shown).

FIG. 5 schematically illustrates the method of combining the reduced recovered product and recycled cooling water. The waste passes through preheater 100 as indicated by arrow 102 to be preheated and passes through nozzle 107
It is guided to the reduction container 104 via.

Now in the reduction vessel 104 the waste is mixed with the gaseous reducing agent through a waste/reductant port 106 provided in the negative region of the vessel. Hydrogen is suitable as this gaseous reducing agent. The reduction vessel 104 includes a ceramic tube 108 and a plurality of holes 110 located in the lower region of the ceramic tube 108, as shown in FIG. Incandescent frame +12 heats reduction container 104. The gaseous reducing agent is directed in a steady but slow flow to the lower region of reduction vessel 104 and inlet 114, as shown in FIG. This population 114 is for forming a barrier that prevents the injection of gaseous waste with water vapor 152, which will be described later. Then, the gaseous waste is placed in the lower region of the reduction vessel, and the hole 1
10 and the inside of the ceramic tube 108 is raised to proceed to the next step.

In the embodiment shown in FIG. 5, the reduced gaseous waste is passed through a retention region 116 with water injection. This treatment method relates to the treatment of halogenated organic waste products. The reduction product is hydrogen halide gas. Water is injected in the form of a mist, and the hydrogen halide gas dissolved or dissociated in the water droplets is concentrated and recovered in tank 11111. The dissolved gas becomes an acid aqueous solution. The tank 11g is provided with a neutralizing agent supply means 120 that controls the amount of acid neutralizing agent injected into the tank. Examples of acid neutralizing agents include bicarbonate, sodium hydroxide, and calcium carbonate. The addition of such an acid neutralizer neutralizes the acid aqueous solution collected in tank 118.

The unconcentrated gas containing the reduction product and water vapor is passed through the cooling pipe 12.
2 to the cooling area 124. These gases are cooled to low temperatures and further concentrated. The cooling temperature in the cooling zone is maintained within a few degrees, and typically above the freezing temperature of the concentrate collected in vessel 128. The remaining unconcentrated gas is passed through region 128 to a demister 130, which is an access control device that captures any remaining droplets or grains. This demister 130 is for capturing any material and discharging it into the container 128.

In the embodiment described above, residual gas is collected using a collection frame (
Flame Arrest) +32 and oxidized in the final step of the treatment method. The propulsion of the gas through the several steps mentioned above is carried out by the peripheral device (Vicinity) 13
This is aided by a fan placed within the 4.

An oxidizing agent such as air or oxygen is injected and mixed with the gas after passing through the collection frame 132.

The gas passing through the oxidation preheating region immediately after passing through the collection frame 132 is preheated before being oxidized in the oxidation region 136 . The oxidizing region 136 is heated, optionally with an oxidizing gas such as natural gas or propane gas, to facilitate oxidation of the residual gas by oxygen and the final product is discharged through the chimney 13g.

The embodiment shown in FIG. 5 uses a heat exchanger 126 in the cooling zone 124 whose emitted energy, along with energy from another heat exchanger 135, is transferred to the gas in the oxidation preheat zone indicated by arrow 125. Used as thermal energy for preheating. Furthermore, a closed area 1 containing water
40 is for recovering the energy released during the oxidation process. The water in the closed area +40 is heated to obtain steam, which is used to assist in preheating the waste in the preheater 100. The flow of water and steam within region 140 is as indicated by arrow 142 in FIG.

In this processing method, the amount of information processing to be controlled, the control valve 1
45 and temperature, most of the acidic gas produced in the reduction process is collected in tank 11g and neutralized. This is at a temperature below and close to the boiling point of water, i.e. between about 70°C and about 100°C, preferably about 85°C.
This can be achieved by maintaining the internal temperature of the retention area 116 to a certain degree.

Certain organic reduction products may be collected as a liquid in tank 118, which may or may not require further processing.

The cooling zone 124 is preferably brought to an extremely lower temperature than the retention zone 116, i.e. to a temperature above and close to the freezing point of the liquid collected in the container 12g, in particular to a temperature of about 20°C, preferably Maintain at approximately 5°C.

As is known to those skilled in the art to which this invention pertains, the organic reduction products concentrated and collected in vessel 128 are, for the most part, easily separable from the aqueous liquid being concentrated. That is, the liquid collected within container 128 generally forms two layers. The first aqueous layer mainly consists of water, and the second organic layer mainly consists of organic reduction products. The aqueous layer is separated and recycled in retention area 116 as indicated by arrow 146 in FIG. The residual organic layer collected in vessel 128 is then purified to remove unnecessary impurities by a distillation operation, a technique other than the distillation operation, or a combination thereof. The purified product thus obtained can be used or sold commercially.

Tank 11 insofar as acid gas is produced in the reduction of the particular organic waste used as feedstock for the present treatment method.
A trapping step for acidic gases generated from the liquid contained in the g is necessary. This trap may not be necessary if the components of the gas vapor from the reduction vessel are directly concentrated and cooled to low temperatures below about 20°C.

Much of the waste is injected into the reduction vessel 104 through the waste/reductant inlet 106, with non-volatile particulate matter being directed to the bottom of the vessel. Such waste is
It is in the form of "pebbles" and is subject to the pebble collection process.

As best shown in FIG. 8, hydrogen inlet 114 is located in the lower region of reduction vessel 104, and
A water (H, O) inlet 150 is arranged below 14 . The pebbles fall into the water vapor 152 and enter the pebble collection tank.
154. This tank 154 automatically opens the valve 15g to empty the tank 154 when the water level reaches a certain height, for example, the mercury level switch 1.
56. Appropriate safety measures include those that ensure detection of blockage of the bottom of reduction vessel 104 by pebbles, malfunction of switch 156, valve 158, etc. The flow discharged from tank 154 is appropriately treated and disposed of.

In other waste injection systems, it is particularly advantageous to treat ash or solid waste using melting methods. Referring to FIG. 9, an electrode 17 is provided in the melting container 170.
2,174, waste inlet +76, slug outlet 178
and a gaseous reducing agent inlet 180 , the interior of the vessel 170 is connected to the retention area 11 via an upper outlet 182 .
6. The waste inlet 176 is equipped with a rotary valve 184,186.

In this system, valve 184 is closed, valve 186 is opened to allow waste 188 to fall into passageway 190, and then
With valve 186 closed and valve 184 open, waste contained within passageway 190 is transferred through waste population 176 to container 170.
let it fall inside. In this way, the ``AEROX SYSTEM'' eliminates the ingress of large amounts of oxygen into the container 170.

The purpose of this valving is to eliminate contact between explosive amounts of oxygen and hydrogen within vessel 170, and other aerodynamic systems suitable for this treatment method may also be employed.

In using this system, a melting material is added to the container 170, which may or may not be part of the waste being treated.

In this system, electricity is passed from one electrode to the other through the heated and melted material. The volatile organic wastes in the melted material are released into a reducing gas atmosphere, usually a hydrogen atmosphere. By controlling the melting process it is possible to provide sufficient heat for use in the reduction process.

In practice, it is desirable to preheat the waste in the waste preheating zone with an oxygen/fuel burner. Typically, the fuel is a hydrocarbon fuel such as methane or natural gas. For example, if there is a power shortage at the location where the waste is being decomposed, it may be desirable to preheat the waste to a higher temperature than is obtainable via the heat exchanger as described above. In such cases, a preheating system such as that schematically shown in FIG. 10 can be used. The preheating system includes a preheating chamber 202, an oxygen supply means 204 having a valve controller 206, a fuel supply means 208 having a valve controller 210,
Oxygen/fuel mixing region 212 and oxygen/fuel ignition means 21
4 to provide a spark to initiate combustion of the oxygen/fuel mixture. For unidirectional injection of waste into the reduction vessel 104 via the nozzle 107, waste supply means 216 with a valve controller 218 and outlet means 220 with an outlet control valve 222 are provided.

In practice, a slight stoichiometric excess of fuel with respect to oxygen is provided so as not to promote oxidation of the waste, and the waste is preheated to a temperature below about 800°C. This preheating system 20
It is of course possible to manage the waste through a preheater 100 shown in FIG.

The description of the embodiments set forth above illustrates the invention, and the invention is not limited to these embodiments or to the additional claims.

[Effects of the Invention] As explained above, according to the present invention, polynuclear aromatic structures contained in organic waste are reduced to a gaseous reaction mixture, and then this mixture is efficiently and reliably decomposed and removed by oxidation. It is possible to do so. Therefore, effects such as decomposition and detoxification of harmful substances in organic waste can be obtained.

[Brief explanation of the drawing]

Fig. 1 is a partially longitudinal sectional front view of the reduction chamber combined with the combustor, Fig. 2 is a partial longitudinal sectional view of the spray nozzle portion of the reduction device, and Fig. 3 is a partial longitudinal sectional view of the reduction chamber combined with the combustor. FIG. 4 is a diagram showing an example of the moving device; FIG. 5 is a diagrammatic layout showing an example of the method according to the invention; FIG. 6 is a diagram showing the upper waste inlet and the inner pipe. A partial longitudinal sectional front view of the equipped reduction container, FIG. 7 is 7-7 in FIG. 6.
8 is a schematic configuration diagram of a pebble collection system used with a reduction chamber; FIG. 9 is a schematic configuration diagram showing an embodiment of the method of the present invention including a melting process that proceeds simultaneously with the reduction process; FIG. 10 is a schematic diagram illustrating an example of a waste preheating system that uses an oxygen/fuel burner prior to reducing the waste. IQ, 104... Reduction container, 12... Metal shell, 14 -... Combustion chamber, 20.27, 107... Nozzle, 21... Liquid inlet, 23... Gas inlet, 24 -・Ceramic insulation, 26 -...
Shell bottom, 28... Auger 30 - Outlet, 32.56... Passage, 36... Exhaust port, 40... Decomposition device, 50... Supply control valve, 54... Variable air inlet Control member, 60・
・Scrubane stem, 6I ・Centrifugal fan particle removal device, 62 ・
・・Cooling shower 65 ・Chimney, 67 ・Neutralized water tank, 69 ・Cooling water tank, 90 ・Low floor trailer, 92 ・Hydraulic a, cutter, 95 ・
...Auxiliary trailer, 100 ...Preheater, 106 ...Waste/reductant inlet, 10g...
・Ceramic tube, 110...hole, 114...inlet, 116...retention area, 118...tank, 120...neutralizer supply means, 122...cooling pipe, 124... Cooling region, 126.135--Heat exchanger, 128--Container, 130--Mist removal device, 132--Collection frame, 134--Peripheral device, 136--Oxidation region, 138 ... Chimney, 140 ... Closed area, 152 - ... Water vapor, 154 ... - Pebble collection tank, 156 ... Mercury level switch, 15g ... Valve, 170 ... Melting container, 172 .174...Electrode, 176...Waste inlet, 17g...Slag outlet, 180...Gaseous reducing agent inlet, 182...Upper outlet, 184.186...Rotary valve, 188
...waste, 190 ... passage, 02 204 06 08 12 14 16 20 22 preheating chamber, ... oxygen supply means, 210.218 ... valve controller, ... fuel supply means, ... oxygen /Fuel mixing area, ...Oxygen/fuel ignition means, ...Waste supply means, ...Outlet means, ...Outlet control valve.

Claims (1)

[Scope of Claims] 1. Direct chemical reduction of organic waste by mixing the waste with a reducing agent, and then heating the waste at about 600° C. in a separate first zone under substantially oxygen-free conditions reduction at a temperature above, transfer the gaseous component obtained by this reduction to a local cooling region within the first region, inject the first aqueous component into the cooling region, and remove the first portion of the gaseous component. liquefying and forming an aqueous phase by cooling and concentrating, collecting the aqueous phase in a collection region, and then injecting a portion of the collected aqueous phase into the cooling region as a first aqueous component; A method for treating organic waste, comprising reusing a part of the aqueous phase. 2. Transferring the reduced gaseous component unidirectionally from the cooling zone to the second zone, and then oxidizing the gaseous component with a gaseous oxidizing agent at a temperature of about 1000° C. or higher. Methods for treating organic waste as described. 3. The method for treating organic waste according to claim 2, characterized in that, before the oxidation treatment, the reduced gaseous component is preheated in a local oxidation preheating region in the second region. 4. The organic waste treatment method according to claim 3, wherein heat is exchanged between the cooling region and the oxidation preheating region. 5. The organic waste treatment method according to claim 1, further comprising washing the lower region of the first region with water and collecting pebbles in the washing liquid. 6. The organic waste of claim 1, wherein the organic waste is preheated in the waste preheating zone to a heating temperature of less than about 200°C, and the organic waste is unidirectionally transferred to the first zone. Processing method. 7. The method for treating organic waste according to claim 6, wherein the heating temperature is about 150°C. 8. After transferring the reduced residual gaseous components from the first region to the second region in a single direction, the gaseous components are heated to about 1000°C.
7. The method for treating organic waste according to claim 6, wherein the oxidation is carried out using a gas oxidizing agent at a temperature above or above. 9. The method for treating organic waste according to claim 8, characterized in that heat is exchanged between the second region and the waste preheating region. 10. The method for treating organic waste according to claim 1, characterized in that the waste is melted within the first region. 11. The method for treating organic waste according to claim 1, characterized in that the internal temperature of the cooling zone is maintained within a range of about 0°C to about 20°C. 12. The method of treating organic waste according to claim 11, characterized in that the internal temperature of the cooling zone is maintained at about 5°C. 13. Injecting a liquid component into a local retention area within the first area;
concentrating a second portion of the gaseous component within the retention zone such that about 1/3 to about 2/3 of the liquid component is concentrated; and concentrating the concentrated component within a localized neutralization zone within the first zone. After compiling,
12. A method according to claim 11, characterized in that the first liquid portion is cooled and concentrated. 14. Concentrating the second portion of the gaseous component such that about 1/2 of the liquid component is concentrated.
Methods for treating organic waste as described. 15. Injecting a liquid component into a local retention area within the first area;
After concentrating a second portion of the gaseous component in the retention zone at a temperature of about 70° C. to about 100° C. and collecting the concentrated component in a neutralization zone in the first zone, 12. A method for treating organic waste according to claim 11, characterized in that the liquid portion is cooled and concentrated. 16. A method for treating organic waste according to claim 15, characterized in that the second portion of the gaseous component is concentrated at a temperature of about 85°C. 17. The gaseous reducing agent is hydrogen, ammonia, neutral gas,
2. The method for treating organic waste according to claim 1, wherein the waste is methane, propane, steam, or a mixture thereof. 18. The method for treating organic waste according to claim 1, wherein the gaseous reducing agent is hydrogen. 19. The organic waste treatment method according to claim 16, further comprising a pre-step of purging the oxygen-containing gas from at least the first region. 20. The method for treating organic waste according to claim 1, wherein the reduction is carried out at a temperature of about 600°C to about 1100°C. 21. The method for treating organic waste according to claim 1, wherein the reduction is carried out at a temperature of about 700°C to about 900°C. 22. The method for treating organic waste according to claim 1, wherein the reduction is carried out at a temperature of about 800°C to about 900°C. 23. The method of claim 1, wherein the waste is reduced in the first region with a residence time of about 0.1 seconds or more. 24. The method for treating organic waste according to claim 1, wherein the waste is reduced with a residence time of about 0.1 seconds to about 45 seconds. 25. The method for treating organic waste according to claim 1, characterized in that the waste is reduced with a residence time of about 5 seconds. 26. The method for treating organic waste according to claim 1, wherein the reduction is carried out using a gaseous reducing agent in the presence of a metal catalyst. 27. The method for treating organic waste according to claim 26, characterized in that the metal catalyst is selected from iron, nickel, zinc, tin and mixtures thereof. 28. The method for treating organic waste according to claim 26, wherein the metal catalyst is iron scrap, powdered nickel, powdered zinc, or powdered tin. 29. The temperature of the thermal reaction mixture obtained by reduction is
The method for treating organic waste according to claim 1, characterized in that the temperature is about 600°C to about 1000°C before injecting the liquid component. 30. The temperature of the thermal reaction mixture obtained by reduction is
The method for treating organic waste according to claim 1, wherein the temperature is about 800°C to about 900°C before the liquid component is injected. 31. Organic wastes are characterized in that they are in the form of liquids, pumped sludges, granular slurries, ground solids, aqueous sediments, shredded or granular organic solids, or inorganic substances contaminated with organic wastes. The method for treating organic waste according to claim 1. 32. The method for treating organic waste according to claim 1, wherein the organic waste contains a halogenated or non-halogenated organic compound. 33. Organic waste includes halogenated biphenyls, halogenated benzenes, halogenated phenols, halogenated cycloalkanes, halogenated alkanes, halogenated dioxins, halogenated dibenzofurans, halogenated alkenes, and halogenated The organic waste according to claim 1, characterized in that it is selected from terpenyls, polynuclear aromatic halogenated hydrocarbons, chlorinated alkenes, or mixed gases, aerosols, and mixtures of gases and aerosols. Processing method. 34. preheating the organic waste to a temperature of about 800° C. or less by burning oxygen and a stoichiometric excess of fuel over the oxygen in the waste preheating zone; A method for treating organic waste according to claim 1, characterized in that the organic waste is transferred unidirectionally to the first area. 35. The method for treating organic waste according to claim 34, wherein the fuel is methane, natural gas, or a mixed gas thereof. 36. directly chemically reducing the organic waste by first intimately mixing it with a gaseous reducing agent and then reducing it in a separate first zone under anoxic conditions at a temperature of about 600° C. or higher;
transferring the reduced gas to a local concentration region within the first region, injecting a liquid component into the concentration region, concentrating and liquefying a portion of the gaseous component within the concentration region to form a liquid phase; After collecting the liquid phase and transferring the remaining reducing gaseous components to the second region,
A method for decomposing organic waste, comprising oxidizing the obtained gaseous mixture with a gaseous reducing agent at a temperature of about 1000° C. or higher. 37. a reduction container; a first gas supply means for supplying purge gas to the container to make the inside of the container an oxygen-free environment;
heating means for raising the temperature within the container to a temperature equal to or higher than a predetermined minimum reducing temperature for a predetermined group of organic waste;
waste supply means for supplying organic waste into a reduction vessel for vaporizing the organic waste in a local mixing region within the reduction vessel; and mixing reducing gas with the organic waste within the mixing region; a first gas supply nozzle means for effectively reducing the organic waste to a reduced gaseous product. 38. Apparatus for decomposing organic waste according to claim 37, characterized in that the reduction vessel is provided with an outlet at its upper position for passing the gaseous products to the outside. 39. The waste supply means is for liquid and granular organic waste, the first gas supply nozzle means having a body portion, an inlet connected to the waste supply means for receiving the waste, and a first gas supply nozzle means having a main body portion and an inlet connected to the waste supply means for receiving the waste; and an axial nozzle for discharging the reducing gas into the body portion as a jet stream, the gas supply nozzle means being directed inward to discharge the reducing gas to collide with the jet stream. The organic waste decomposition device according to claim 38. 40. A combustion vessel adjacent to the reduction vessel, and a flow control transfer passage connecting the reduction vessel outlet to the combustion vessel to unidirectionally transfer the reduced gaseous product from the reduction vessel to the combustion vessel for exothermic combustion. Claim 3 characterized in that it comprises means.
8. The organic waste decomposition device according to 8. 41, characterized by comprising scrubber means for receiving liquid combustion products from the combustion vessel and scrubbing the products with an alkaline solution having a predetermined pH value to substantially neutralize the acid content of the combustion products; The organic waste decomposition apparatus according to claim 40. 42. Claim 40 characterized by comprising an electric energy generation means for receiving hot gas from combustion in an electricity generation relationship.
Decomposition equipment for organic waste as described. 43. The organic waste decomposition apparatus of claim 42, wherein said electrical energy generating means includes a boiler for receiving said hot gas connected in driving relation to an alternating current generator. 44. A combustion vessel adjacent to the reduction vessel, and a flow control transfer passage connecting the reduction vessel outlet to the combustion vessel to unidirectionally transfer the reduced gaseous product from the reduction vessel to the combustion vessel for exothermic combustion. Claim 3 characterized in that it comprises means.
9. The organic waste decomposition device according to 9. 45. A waste supply means and a first gas supply nozzle means are disposed in the upper region of the reduction vessel, and an access control which is an extension passage between the waste supply means and the flow control transfer passage means is provided in the reduction vessel. 45. The organic waste decomposition apparatus according to claim 44, further comprising a means for decomposing organic waste. 46. A cooling vessel having a first cooling means adjacent to the reduction vessel, and a transfer for transferring the reduced gaseous product from the reduction vessel to the cooling vessel for the cooling process by connecting the reduction vessel outlet to the cooling vessel. 46. The organic waste decomposition apparatus according to claim 45, further comprising passage means. 47. A neutralization tank having a liquid injection means, a liquid collection means, and a neutralizing agent supply means, and connected to the transfer passage means and disposed between the outlet of the reducing container and the cooling container. 47. The organic waste decomposition apparatus according to claim 46. 48. A cooling vessel having a first cooling means adjacent to the reduction vessel, and a first cooling vessel with a reduction vessel outlet connected to the cooling vessel for transferring the reduced gaseous product from the reduction vessel to a cooling vessel for the cooling process. 39. The organic waste decomposition apparatus according to claim 38, further comprising: 1 transfer passage means. 49. The cooling container includes a liquid injection means, a liquid collection means disposed below the liquid injection means, and a transfer means for transferring the liquid from the collection means to the injection means. 49. The organic waste decomposition apparatus according to claim 48. 50. A combustion vessel adjacent to said cooling vessel and a flow controlled transfer connecting said cooling vessel to said combustion vessel for unidirectionally transferring reduced gaseous products from said cooling vessel to said combustion vessel for exothermic combustion. 50. The organic waste decomposition apparatus according to claim 49, further comprising passage means. 51. The organic waste decomposition apparatus according to claim 50, further comprising an oxidizing preheating vessel disposed between the flow control transfer passage means and the combustion vessel. 52. The apparatus for decomposing organic waste according to claim 51, further comprising a first heat transfer means for transferring the energy released during the cooling step to the preheating vessel for oxidation. 53. A neutralization tank having a liquid injection means, a liquid collection means, and a neutralizing agent supply means, and connected to the first transfer passage means and disposed between the outlet of the reduction container and the cooling container. 53. The organic waste decomposition apparatus according to claim 52, further comprising: 54. The organic waste according to claim 53, further comprising a waste preheating container connected to the waste supply means and having preheating means for preheating the organic waste before passing through the supply means. A device for disassembling things. 55. The organic waste decomposition apparatus according to claim 54, wherein the preheating means includes a second heat transfer means connected to the combustion vessel and the second preheating vessel. 56. The organic waste decomposition apparatus according to claim 55, wherein the second heat transfer means includes means for circulating water and steam. 57. A neutralization tank having a liquid injection means, a liquid collection means, and a neutralizing agent supply means; the outlet of the reduction container is connected to the neutralization tank, and the reduced gaseous product is discharged from the reduction container. 39. The organic waste decomposition apparatus according to claim 38, further comprising transfer passage means for transferring the organic waste to a neutralization tank. 58. The organic waste decomposition apparatus according to claim 37, wherein the heating means includes a melting means. 59. Claim 3, further comprising a waste preheating container connected to the waste supply means and having preheating means for preheating the organic waste before passing through the supply means.
7. The organic waste decomposition device according to 7. 60, an outlet provided above the reduction vessel for passing the gaseous product outward; a combustion vessel adjacent to the reduction vessel; and a combustion vessel configured to connect the outlet of the reduction vessel to the combustion vessel to generate the reduced gas. 60. The organic waste decomposition apparatus of claim 59, further comprising flow control transfer passage means for unidirectionally transferring the product from the reduction vessel to the combustion vessel for exothermic combustion. 61. The apparatus for decomposing organic waste according to claim 60, characterized in that the preheating means comprises heat transfer means for transferring the energy released during exothermic combustion to the waste preheating container. 62. The organic waste decomposition apparatus according to claim 61, wherein the heat transfer means includes means for circulating water and steam. 63. Claim 4, further comprising a pebble collecting means disposed below the waste supply means and the access control means.
5. The organic waste decomposition device according to 5. 64. The organic waste decomposition apparatus according to claim 63, wherein the pebble collecting means includes a liquid inlet and a collection tank. 65. An apparatus for decomposing organic waste as claimed in claim 64, characterized in that the collection tank is provided with downward valve means for transferring liquid and gravel from the tank. 66. The waste preheating container according to claim 34, further comprising a waste preheating container connected to the waste supply means and having a preheating means for preheating the organic waste before passing through the supply means. Organic waste decomposition equipment. 67. An apparatus for decomposing organic waste according to claim 66, characterized in that the preheating means comprises an oxygen/hydrocarbon fuel burner.