JPH09201590A - Simultaneous treatment of organic solid waste and liquid waste - Google Patents

Abstract

PROBLEM TO BE SOLVED: To collectively treat org. solid waste and water with high decomposition efficiency and to recover power or heat energy. SOLUTION: This treatment method is composed of a process of subjecting a liquid mixture of org. solid waste and liquid waste to wet oxidation treatment in the presence of oxygen in a first reactor at 100 deg.C or higher while holding pressure keeping a liquid phase, a process of removing formed sludge and/or a metal component from the first reactor, a process of subjecting a high temp. and high pressure treated liquid to gas-liquid separation, a process of removing sludge and/or a metal component from the liquid phase and mixing a part of the liquid phase with the liquid waste to circulate the same to the first reactor and a process of subjecting the remainder of the liquid phase and the gas phase to catalytic wet oxidation treatment at liquid linear velocity of 0.1cm/sec or more at 100 deg.C or higher under pressure keeping a liquid phase.

Description

Detailed Description of the Invention

[0001]

TECHNICAL FIELD The present invention relates to an organic solid waste.
(Garbage, paper, plastic, wood pieces, bamboo pieces, grass pieces, straw, fibers, vegetable pieces, rubber, skins, etc.) and liquid waste (aerobic sludge, anaerobic sludge, sewage sludge, etc.); life Wastewater, wastewater from food factories, industrial wastewater containing components that are difficult to biologically treat, etc.).

[0002]

2. Description of the Related Art Conventional sludges, various kinds of waste water, and solid wastes containing organic substances are conventionally treated by different techniques according to their characteristics.

For example, sludge is dehydrated and then incinerated or landfilled. The organic matter-containing wastewater is treated with activated sludge, and the generated sludge is incinerated or landfilled as described above. Solid waste containing organic substances is incinerated as it is or after being dried.

However, in recent years, the amount of various kinds of waste generated has increased, and it is gradually becoming difficult to deal with the above-mentioned methods of individually treating by the conventional technique.

[0005]

Therefore, the present invention provides a new technique capable of collectively treating organic solid waste and wastewater with high decomposition efficiency and recovering electric power, thermal energy and the like. The main purpose is that.

[0006]

In view of the current state of the art as described above, the inventor of the present invention has started a study on a technology for treating sludges, various waste waters, organic solid wastes and the like. In the process, mixing organic solid waste and liquid waste,
It has been found that when the wet oxidation treatment and the catalytic wet oxidation treatment are carried out under a specific condition, the above problems can be almost achieved.

That is, the present invention provides a method for simultaneously treating the following organic solid waste and liquid waste: I. (1) In the first reactor, while maintaining the liquid mixture of the organic solid waste and the liquid waste at a temperature of 100 ° C. or higher and at a pressure for maintaining the liquid phase, a cyanide compound and a nitrogen compound in the liquid mixture A step of performing a wet oxidation treatment in the presence of oxygen in an amount equal to or more than the theoretical oxygen amount necessary for decomposing organic substances and inorganic substances, (2) adding sludge and / or metal components produced in the step (1) above A step of removing from the one reactor, (3) a step of gas-liquid separation of the high temperature and high pressure treatment liquid obtained in the step (1) above, (4) a liquid phase obtained in the step (3) above After removing the sludge and / or metal components, a part of the liquid phase is mixed with the liquid waste and circulated in the first reactor, and the remainder of the liquid phase is sent to the step (5) below. And (5) in the second reactor, the step of (4) above. The residue of the liquid phase from which sludge and / or metal components have been removed and the gas phase obtained in the above step (3) are mixed in the presence of a catalyst containing at least one metal or metal compound as an active ingredient. A linear wettability (amount of liquid fed / reactor cross-sectional area) of 0.1 cm / sec or more, a temperature of 100 ° C. or more, and a pressure for maintaining the liquid phase of the treatment liquid, while carrying out a catalytic wet oxidation treatment step. Characteristic method for simultaneous treatment of organic solid waste and liquid waste.

2. Item 1. The amount of the liquid phase circulated from the step (4) to the first reactor is 5 times or more the amount of the liquid phase fed from the step (4) to the step (5). Simultaneous treatment method of organic solid waste and liquid waste.

3. Item 3. The amount of the liquid phase circulated from the step (4) to the first reactor is 10 to 20 times the amount of the liquid phase fed from the step (4) to the step (5). Method for simultaneous treatment of organic solid waste and liquid waste of.

4. The catalytically active component in step (5) is
The above items 1 to 3 which are at least one selected from the group consisting of iron, cobalt, nickel, ruthenium, rhodium, palladium, iridium, platinum, copper, gold and tungsten, and compounds of these metals which are insoluble or sparingly soluble in water.
4. The method for simultaneously treating organic solid waste and liquid waste according to any one of 3 above.

5. The organic solid waste and liquid waste according to any one of the above items 1 to 4, wherein power and / or steam or hot water is recovered from a mixed gas of steam and exhaust gas separated from the liquid at the outlet of the second reactor. Simultaneous processing method with.

[0012]

BEST MODE FOR CARRYING OUT THE INVENTION Examples of organic solid wastes to be treated by the present invention include vegetation, bamboo, grass, straw, fibers, vegetable waste, rubber, and hide. The liquid waste is not particularly limited, and sludge such as aerobic treated sludge, anaerobic treated sludge, and sewage sludge; domestic wastewater including kitchen waste, paper, plastic, human waste, plating wastewater, food factory wastewater,
Paper mill wastewater, pharmaceutical factory wastewater, photographic wastewater, printing wastewater, agricultural chemicals-related wastewater, dyeing wastewater, semiconductor manufacturing factory wastewater, wastewater generated by coal liquefaction or gasification, wastewater generated by thermal decomposition of municipal waste, etc. Examples include wastewater containing organic substances. These organic solid wastes and liquid wastes, if necessary, may be used by mixing two or more of each,
You may process.

The organic solid wastes and / or liquid wastes to be treated by the present invention further include Mg, Al and S.
i, P, Ca, Ti, Cr, Mn, Fe, Co, Ni,
It may contain one kind or two or more kinds of metal components such as Cu, Zn and Cd.

The present invention will be described in detail below with reference to the drawings.

FIG. 1 is a flow sheet showing the outline of the present invention.

The liquid waste is pressurized to a predetermined pressure by a pressure pump, further mixed with an oxygen-containing gas such as air which has been pressurized in advance by a compressor, and then heated to a temperature of 100 ° C. or higher by a heat exchanger. After that, it is supplied to a first reactor (hereinafter, referred to as an empty column reactor in order to distinguish it from a second reactor filled with a catalyst described later) together with a circulating liquid phase described later.

On the other hand, the organic solid waste is supplied to the empty column reactor as shown in FIG. That is, before the start of the operation of charging the organic solid waste, the valves 1, 2 and 3 of the charging device are closed, the pressure inside the empty column reactor is high, and the pressure inside the charging device is normal pressure. When the charging operation is started, the valve 1 is opened, the solid waste is charged into the charging device, the valve 1 is closed, the valve 3 is opened, and the pressure inside the charging device is increased to the same pressure as the empty column reactor by high pressure air. To do. Next, the valve 3 is closed, the valve 2 is opened, the solid waste in the charging device is charged into the empty column reactor, and then the valve 2 is closed.
At this time, if the size of the solid waste is too large, it is crushed or crushed in advance before being supplied to the charging device.

As a heat source of the heat exchanger, a high-temperature treatment liquid from a second catalyst-filled reactor (hereinafter, referred to as a catalyst reactor for distinguishing from the first superficial reactor) is circulated. Or other heating means may be used. If the concentration of pollutants is low and the prescribed reaction temperature cannot be maintained during the reaction, such as in winter, or if it is necessary to raise the temperature to the prescribed temperature, then use a heater (not shown) to further heat it, Alternatively, steam can be supplied to the superficial reactor from a steam generator (not shown). Further, in order to bring the temperature inside the superficial reactor to a predetermined temperature at the time of start-up, steam is directly fed into the supercritical reactor to raise the temperature, or between the heat exchanger and the superficial reactor. A heater (not shown) may be provided to raise the temperature.

The temperature in the reaction (first reaction) in the empty column reactor is usually about 100 ° C. or higher, more preferably 150 to 37.
It is about 0 ° C. The higher the temperature during the reaction, the higher the decomposition rate of organic substances, etc., and the shorter the residence time of the material to be treated (liquid waste + organic solid waste + circulating liquid phase) in the empty column reactor, On the other hand, since the equipment cost increases, the primary reaction temperature can be set by comprehensively considering the concentration of pollutant in the object to be treated, the required degree of treatment, operating cost, construction cost, etc. . The pressure at the time of reaction may be equal to or higher than the pressure at which the object to be treated can maintain the liquid phase at a predetermined temperature.

The amount of oxygen added to the material to be treated is at least the theoretical oxygen amount necessary for decomposing the cyan compounds, nitrogen compounds, organic substances and inorganic substances into harmless products, more preferably the theoretical oxygen amount. 1.05 to 1.5 times the amount.

FIG. 1 shows an embodiment in which air is used as the oxygen source, but the oxygen source is not particularly limited,
Other examples include oxygen-enriched air, oxygen, and oxygen-containing waste gas containing one or more of hydrogen cyanide, hydrogen sulfide, ammonia, sulfur oxides, organic sulfur compounds, nitrogen oxides, hydrocarbons, etc. as impurities. To be done.

In the present invention, the theoretical amount of oxygen means "cyan compounds, nitrogen compounds, organic substances and inorganic substances (components to be treated) in the water-containing waste are N ₂ , H ₂ O and CO ₂
Means the amount of oxygen required to decompose to. The theoretical oxygen amount can be calculated easily by analyzing the components to be treated in the mixture to be treated (liquid waste + organic solid waste + circulating liquid phase) and calculating the theoretical oxygen amount required for their decomposition. You can decide. In practice, based on experience and some experimentation,
With some parameters, it is possible to find a relational expression that can approximately calculate the theoretical oxygen amount with high accuracy.
Such a relational expression is disclosed in, for example, Japanese Patent Publication No. 58-27999.

In the lower part of the superficial column reactor, as time passes, sludge mainly composed of inorganic compounds is settled and deposited. As for the accumulated sludge, as shown in the lower part of FIG. 2, after opening the valve 4 below the empty column reactor and transferring the sludge liquid in the reactor to the sludge discharge device, the valve 4 was closed and then the valve 5 was closed. It can be removed by opening it. Depending on the type of liquid waste (for example, when the liquid waste is plating waste water and cyan is produced), steam is supplied to the sludge discharge device to completely remove the cyan in the sludge. Can be decomposed into Since sludge and / or metal components are gradually deposited on the sludge discharging device, the valve 5 provided below the sludge discharging device is opened to discharge the sludge liquid, and then the valve 5 is closed. The sludge liquid can be subjected to a known solid-liquid separation treatment, and the separated liquid can be recycled together with the liquid waste to the empty column reactor for treatment. The sludge generated in the superficial column reactor can be semi-continuously withdrawn and discharged by such a lock hopper system. By removing the sludge and / or the metal component, it is possible to suppress the adhesion to the catalyst in the subsequent catalytic reactor and maintain the high catalytic activity for a long period of time.

Needless to say, the sludge discharge device shown in FIG. 2 can also be used in the empty column reactor of FIG. 1 or FIG. 4 described later.

The primary treatment liquid formed in the empty column reactor is
It is separated into a liquid phase and a gas phase.

FIG. 3 schematically shows an example of the gas-liquid separation device in the empty column reactor. In the apparatus shown in the figure, a gas-liquid separator equipped with four nozzles N-1, N-2, N-3 and N-4 is provided above the empty column reactor, and the gas-liquid separator from the bottom of the reactor is installed. The mixture (G + L) is separated at the nozzle N-1. The gas phase G is
It is guided to the next step from the upper part of the liquid surface or nozzle N-2 through nozzle N-3. On the other hand, the liquid phase L is from the nozzle N-1 to the nozzle N-4.
And is led to the next step. The separated liquid phase L is supplied to a solid-liquid separator, where solids are removed, and then the gas phase
It is supplied to the second catalytic reactor together with G and used for the secondary reaction. In the present invention, gas-liquid separation in the superficial column reactor can be carried out by using an apparatus having an arbitrary configuration as long as the object can be achieved.

The solid-liquid separation device is used to separate solid substances that have not been precipitated and removed in the empty column reactor, and a ceramic filter, a metal filter, a cyclone device, etc. may be used alone or in appropriate combination. To do.
Although not shown, it is preferable that two solid-liquid separators are installed, valves are switched, and they are used alternately. When installing two series of solid-liquid separators, one series in an unused state is chemically (for example, 5 to 10) under normal pressure or under pressure.
Cleaning with chemicals such as% nitric acid, 5-10% sodium hydroxide) or physically (using steam or high pressure steam or moving ceramic balls, metal balls, etc.) As a result, sludge can be removed from the system. By using the solid-liquid separation device, it is possible to effectively remove the solid content in the liquid phase from the superficial reactor, so that the activity of the catalyst filled in the catalytic reactor can be stabilized over a long period of time. It can be sustained and its life can be extended.

The liquid phase is supplied to a solid-liquid separator, where solids are removed, and then a part of the liquid phase is circulated to the empty column reactor together with the liquid waste, and the rest is combined with the gas phase in the first phase. It is supplied to the second catalytic reactor and used for the secondary reaction.

The amount of the liquid phase circulated from the solid-liquid separator to the empty column reactor is about 5 times or more the amount of the liquid phase fed from the solid-liquid separator to the catalytic reactor (more preferably 10%). Approximately 20 times; hereinafter, this circulation amount / feeding amount ratio is referred to as a circulation ratio). By circulating this liquid phase that still contains a small amount of undecomposed solid content, the solubilization reaction in the superficial reactor is promoted, and the activity of the catalyst packed in the catalytic reactor is maintained for a longer period of time. The life can be further extended.

When a large amount of alkali metal compound derived from liquid waste and / or organic solid waste is contained in the liquid phase fed from the solid-liquid separation device to the catalytic reactor, it is in the liquid phase. 0.25 to 0.55 per 1 mol of total alkali metal
It is preferable to adjust the pH by adding a double amount of sulfuric acid. The addition of this sulfuric acid can also suppress the production of nitrogen compounds (particularly NO ₂ -type nitrogen and NO ₃ -state nitrogen) in the catalytic reactor. Instead of sulfuric acid or together with sulfuric acid, a substance capable of generating sulfuric acid under the reaction conditions in the catalytic reactor (for example, sulfur, a sulfur compound such as ammonium thiosulfate) may be added. In the present invention, the term "sulfuric acid" is intended to include these "sulfuric acid forming substances".

Also in the second reaction, when the pollutant concentration is low and the predetermined reaction temperature cannot be maintained during the reaction in winter or the like, heating is performed by a heater (not shown) or a steam generator (see FIG. It is also possible to supply steam to the catalytic reactor from (not shown). Further, in order to bring the inside of the catalytic reactor to a predetermined temperature at the time of start-up, the high temperature primary treatment liquid from the superficial reactor is circulated to raise the temperature, or steam is directly fed into the catalytic reactor. To raise the temperature,
Alternatively, the temperature can be raised by a heater (not shown).

The difference between the superficial column reactor and the catalytic reactor is that the latter is filled with the catalyst supported on the carrier and that the liquid linear velocity in the latter is 0.1 cm / sec or more.

Examples of the catalytically active component include iron, cobalt, nickel, ruthenium, rhodium, palladium, iridium, platinum, copper, gold and tungsten, and water-insoluble or sparingly water-soluble compounds of these metals. More specific examples of such compounds include oxides (cobalt oxide, iron oxide, etc.), chlorides (ruthenium dichloride,
Platinum dichloride, etc.), sulfides (ruthenium sulfide, rhodium sulfide, etc.) and the like. These metals and their compounds may be used alone or in combination of two or more kinds. These catalytically active components are used in a state of being supported on a known metal oxide carrier and metal carrier according to a conventional method. The metal oxide support and metal support are not particularly limited, and those used as known catalyst supports can be used. As the metal oxide carrier,
Alumina, silica, zirconia, titania, composite metal oxides containing these metal oxides (alumina-silica, alumina-silica-zirconia, titania-zirconia, etc.), metals containing these metal oxides or composite metal oxides as main components Examples thereof include oxide-based carriers, and examples of metal carriers include iron and aluminum. Among these carriers, zirconia, titania and titania-zirconia, which have excellent durability, are more preferable.

The shape of the supported catalyst is not particularly limited, and examples thereof include a spherical shape, a pellet shape, a cylindrical shape, a crushed piece shape, a powder shape, and a honeycomb shape. The volume of the reactor in the case of using such a supported catalyst packed is such that, in the case of a fixed bed, the space velocity of the liquid is about 0.5 to 10 hr ^-1 , more preferably about ¹ to 5 hr ^-1 . Is good. The size of the supported catalyst used in the fixed bed is usually 3 to 50 mm, more preferably 5 to 25, in the case of spherical, pellet-shaped, columnar, crushed piece-shaped, powdered, etc.
mm. When the catalyst is supported on a honeycomb-shaped carrier and used, a honeycomb structure having an opening having an arbitrary shape such as a square, a hexagon or a circle is used. The area per unit volume, the aperture ratio, etc. are not particularly limited, but usually 200 as the area per unit volume.
~ 800m ² / m ³ , use an aperture ratio of 40 ~ 80%.
As the material of the honeycomb structure, the same metal oxides and metals as the above are exemplified, and zirconia having excellent durability,
More preferred are titania and titania-zirconia.

When the fluidized bed is formed in the catalytic reactor, the amount of the supported catalyst that can form the fluidized bed in the reactor, that is, usually about 0.01 to 20%, more preferably based on the weight of the liquid phase, is more preferable. Is used by suspending about 0.05 to 10% in a liquid phase in a slurry form. When using a fluidized bed, the supported catalyst is supplied to the catalytic reactor in a state of being suspended in a slurry in the liquid phase, and the catalyst is precipitated from the secondary treatment liquid discharged outside the tower after the reaction is completed. , Collect by appropriate method such as centrifugation, and reuse. Therefore, considering the ease of separation and recovery of the catalyst from the secondary treatment liquid, the particle size of the supported catalyst used in the fluidized bed is more preferably about 0.15 to 0.5 mm. The amount of the catalytically active metal supported is not particularly limited, but it is usually in the range of about 0.01 to 25% by weight of the carrier, more preferably about 0.1 to 3%.

The reaction temperature in the catalytic reactor is 100 ° C. or higher. By the primary treatment in the superficial reactor, the organic matter in the material to be treated is solubilized and the reactivity is increased, so the reaction temperature in the catalytic reactor is 10 ° C or higher than the reaction temperature in the superficial reactor. Can be lowered. Further, in the empty column reactor, sludge and / or metal components contained in the object to be treated are efficiently removed, and further, the solid content is also removed in the solid-liquid separation device, It is also prevented that the activity of the catalyst packed in the catalytic reactor is disturbed.

Treatment liquid from the catalytic reactor (secondary treatment liquid)
After being used as a source of heat for raw water in the heat exchanger as described above, it is sent to the gas-liquid separator via the heat recovery device for recovering the residual heat energy as steam and / or hot water. It is separated into a phase (exhaust gas) and a liquid phase (treated water).

Although not shown, the liquid phase obtained from the secondary treatment liquid is, if necessary, further sent to a solid-liquid separator by a conventional method, and the metal and / or sludge components contained in the liquid phase are added. After being removed, it becomes the final treatment liquid. As a separation method in the solid-liquid separator, known methods such as separation by gravity settling, separation by a magnet, separation by a filter press, and separation by coagulating sedimentation can be adopted.

Since the gas phase (exhaust gas) does not substantially contain ammonia, nitrogen oxides, sulfur oxides, dioxins, etc., it can be directly emitted to the atmosphere.

Further, in the first invention of the present application, as shown in FIG. 4, the mixed gas of the vapor and the exhaust gas separated from the liquid in the upper part of the catalytic reactor is introduced as it is to a power recovery device such as an expansion turbine to generate power. Collection can be performed. further,
It is also possible to recover heat from the high temperature and high pressure exhaust gas and the treatment liquid in the form of steam. In these cases, the recovered power can recover power exceeding the power consumption of the air compressor, the pump, and the like. Note that, in FIG. 4, the same constituent elements as those in FIG. 1 (for example, an empty column reactor, etc.)
Regarding, the description of the name is omitted.

[0041]

According to the method of the present invention, organic solid waste and liquid waste can be efficiently treated at the same time.

Further, ammonia, nitrogen oxides, organic substances and inorganic substances in the liquid waste are substantially completely decomposed, so that a stable treatment effect is achieved.

The presence of harmful components is not substantially observed in both the gas phase and the liquid phase (final treatment liquid) after the final gas-liquid separation.

When an oxygen-containing waste gas is used as an oxygen source, the presence of harmful components derived from the waste gas is not substantially recognized in either the gas phase or the liquid phase.

The sludge formed is excellent in sedimentation and easy to handle.

According to the method of the present invention, each process is continuously carried out and the processing flow is extremely simple, so that the processing cost (equipment cost, operating cost, etc.) is remarkably reduced and the process control becomes easy.

Further, electric power and / or heat can be efficiently recovered from the high temperature and high pressure exhaust gas and the treatment liquid.

[0048]

EXAMPLES Examples and comparative examples are shown below to further clarify the features of the present invention.

Example 1 In accordance with the flow chart shown in FIG. 1, according to the present invention, kitchen waste (composition ratios shown in Table 1), plastic waste material (composition ratios shown in Table 2), paper waste material (composition components shown in Table 3). Ratio), other combustible waste materials (Table 4 shows the component ratio)
And 100 parts by weight of a solid waste mixture (composition ratio shown in Table 6) consisting of sludge (composition shown in Table 5) and sewage treatment plant wastewater (composition shown in Table 7; hereinafter referred to as raw water) The processed object (solid content concentration 10% by weight) was processed. The garbage was crushed by a disposer, and the other solid wastes were crushed by a crusher in advance and then mixed.

[0050]

[Table 1]

[0051]

[Table 2]

[0052]

[Table 3]

[0053]

[Table 4]

[0054]

[Table 5]

[0055]

[Table 6]

[0056]

[Table 7]

That is, the solid waste mixture was supplied to the empty column reactor by the raw material charging device and the raw water was supplied by the pump to the processed object (2.2 m ³ / m ² / hr) formed from the compressor. Air corresponding to 1.1 times the theoretical oxygen amount (31.5 Nm ³ / kl) was supplied.

In the reaction, raw water and air are introduced into the inlet side of the heat exchanger, and the temperature of the gas-liquid mixture at the outlet side of the heat exchanger (the inlet side of the superficial column reactor) is 270 ° C. Then, the secondary treatment liquid from the catalytic reactor was sent to the heat exchanger to exchange heat with the gas-liquid mixture, and the temperature was adjusted.
The inside of the superficial column reactor was maintained at a temperature of 270 ° C. and a pressure of 86 Kg · cm ⁻² G by wet oxidative decomposition of organic matter in the material to be treated.

To remove the sludge and / or metal components formed in the empty column reactor, the first valve provided at the lower part of the reactor is opened to transfer the sludge liquid in the empty column reactor to the sludge discharge device. After that, close the first valve, cool,
This was done by opening a second valve provided at the bottom of the sludge discharge device to discharge the sludge liquid.

Then, after the obtained primary treatment liquid was separated into gas and liquid, the liquid phase (liquid phase-1) was introduced into a solid-liquid separator to remove solids.

Then, most of the liquid phase-2 obtained by the above solid-liquid separation (22 m ³ / m ² / hr; therefore, circulation ratio = 10 times)
Of the residual (2.2m ³ / m ²
/ hr) was supplied to the catalytic reactor at a liquid space velocity of 0.67 hr ^-1 (vacant column standard) together with the gas phase obtained by gas-liquid separation, and catalytic wet oxidation was performed. The catalyst reactor is filled with a spherical catalyst (diameter 4-6 mm) in which 2% of the weight of the carrier is ruthenium supported on the titania carrier, and the internal temperature and pressure are almost the same as those of the empty column reactor. Held in. The liquid linear velocity in the catalytic reactor was 0.06 cm / sec.

Table 8 shows the composition of the liquid phase-1, liquid phase-2, and the secondary treatment liquid from the catalytic reactor.

[0063]

[Table 8]

Note: The amounts of metals in Table 8 are Al, Fe, Ca, Mg,
P, Mn, Zn, Cu, Ni, Cr, Pb, Cd, Sr, Ba, Co and Mo
The total amount of

Cadmium, chromium, lead, mercury and their compounds were not detected in the secondary treatment liquid. The exhaust gas is ammonia, NO _x , SO _x ,
Substantially no O ₂ , N ₂ and C without dioxin etc.
It consisted of O ₂ .

Examples 2 to 14 The waste mixture was treated in the same manner as in Example 1 except that the active ingredient / catalyst support combination of the catalyst charged in the catalytic reactor was variously changed. Table 9 shows the results.

[0067]

[Table 9]

From the results shown in Table 9, it is clear that even when the active component / support combination of the catalyst was changed, excellent effects were achieved in the wet oxidation treatment of the waste mixture.

Example 15 After preliminarily adjusting the solid content concentration of the waste mixture to 10%, the waste mixture was treated according to the flow shown in FIG. 4 and under the same reaction conditions as in Example 1. .

That is, after performing the wet oxidation of the waste mixture in the same manner as in Example 1, the mixed gas of the steam and the exhaust gas separated from the treatment liquid in the upper part of the catalytic reaction tower is guided to the expansion turbine to recover the power. As a result, it was possible to recover power exceeding the power consumption of the air compressor, booster pump, etc.

[Brief description of drawings]

FIG. 1 is a flow sheet showing an outline of the present invention.

FIG. 2 is a flow sheet showing an outline of a solid waste supply mechanism and a sludge discharge mechanism to a superficial reactor used in the present invention.

FIG. 3 is a schematic diagram showing an outline of an example of a gas-liquid separation device installed in the empty column reactor.

FIG. 4 is a flow sheet showing an outline of the case of performing power recovery in the present invention.

[Explanation of symbols]

 1 ... Solid waste supply control valve 2 ... Supply control valve from raw material charging device to empty column reactor 3 ... High pressure air supply control valve 4 ... Sludge discharge control valve from empty column reactor 5 ... From sludge discharge device Sludge discharge control valve N-1 ... Nozzle N-2 ... Nozzle N-3 ... Nozzle N-4 ... Nozzle

─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. ⁶ Identification code Office reference number FI Technical indication location B01J 23/46 B01J 23/46 M 301 301M 23/52 23/52 M 23/72 23/72 M 23/745 27/057 M 23/75 C02F 1/58 CDCN 23/755 CDHP 27/057 CDVA B09B 5/00 ZAB 11/08 ZAB C02F 1/58 CDC B01J 23/74 301M CDH 311M CDV 321M 11/08 ZAB B09B 5/00 ZABM (72) Inventor Nobuyuki Matsumoto 4-1-2, Hirano-cho, Chuo-ku, Osaka City Osaka Gas Co., Ltd. (72) Suewa Yamada 4-1-2, Hirano-cho, Chuo-ku, Osaka In Gas Co., Ltd. (72) Kenichi Yamazaki Inventor Kenichi Yamazaki 4-1-2 Hirano-cho, Chuo-ku, Osaka City Osaka Gas Co., Ltd.

Claims (5)

[Claims] (1) In a first reactor, a liquid mixture of an organic solid waste and a liquid waste is kept at a temperature of 100 ° C. or higher and at a pressure for maintaining a liquid phase, while Wet oxidation treatment in the presence of oxygen in excess of the theoretical oxygen amount required for decomposing cyanide compounds, nitrogen compounds, organic substances and inorganic substances, (2) sludge produced in the above step (1) and / or Alternatively, the step of removing the metal component from the first reactor, (3) the step of separating the high-temperature and high-pressure treatment liquid obtained in the step (1) from gas-liquid, (4) the above (3)
After removing sludge and / or metal components from the liquid phase obtained in the step of (1), a part of the liquid phase is mixed with the liquid waste and circulated in the first reactor, and the residual liquid phase is In the step of feeding to the step (5), and (5) in the second reactor, the residue of the liquid phase from which the sludge and / or the metal component has been removed in the step of the above (4) and the step of the above (3) Liquid phase velocity (amount of liquid fed / reactor cross-sectional area) of 0.1 cm / sec or more in the presence of a catalyst containing at least one of a metal and a metal compound as an active ingredient, and 100 While maintaining the temperature above ℃ and the pressure that the processing liquid maintains the liquid phase,
A method for simultaneously treating organic solid waste and liquid waste, comprising a step of catalytic wet oxidation treatment. 2. The amount of the liquid phase circulated from the step (4) to the first reactor is at least 5 times the amount of the liquid phase fed from the step (4) to the step (5). Item 2. A method for simultaneously treating organic solid waste and liquid waste according to Item 1. 3. The amount of liquid phase circulated from step (4) to the first reactor is 10 to 20 times the amount of liquid phase fed from step (4) to step (5). The method for simultaneously treating the organic solid waste and the liquid waste according to claim 2. 4. The catalytically active component in step (5) is iron,
4. At least one selected from the group consisting of cobalt, nickel, ruthenium, rhodium, palladium, iridium, platinum, copper, gold and tungsten, and water-insoluble or sparingly soluble compounds of these metals. A method for simultaneously treating an organic solid waste and a liquid waste according to Crab. 5. The organic solid waste according to any one of claims 1 to 4, wherein power and / or steam or hot water is recovered from a mixed gas of steam and exhaust gas separated from the liquid at the outlet of the second reactor. Method for the simultaneous treatment of waste and liquid waste.