JPH0478496A - Treatment of waste water and sludge - Google Patents

Abstract

PURPOSE:To hygienically, economically and efficiently treat crude waste, etc., by mixing separated solids with waste water, subjecting the resulted mixture to an oxidation decomposition by a wet process in the presence of oxygen, and subjecting the mixture to the oxidation decomposition by a wet process in the presence of a honeycomb-shaped carrier catalyst and oxygen. CONSTITUTION:Garbage, etc., are ground to a slurry form and are mixed with living waste water, etc. The mixture is discharged to an exclusively used drain pipe. The solids and liquid components in the above-mentioned mixture are decomposed and the separated liquid components are subjected to an activated sludge treatment. On the other hand, the separated solids and the solids, etc., generated in a sewage treatment plant are mixed with sewage or waste water. The resulted mixture is subjected to the oxidation decomposition by the wet process at about pH 1 to 11.5 and 100 to 370 deg.C. The treated liquid obtd. in such a manner is subjected to the oxidation decomposition by the wet process at about pH 1 to 11.5 and 100 to 370 deg.C in the presence of the honeycomb-shaped carrier catalyst consisting of at least one kind of noble metals and base metals as the active component and in the presence of the oxygen of 1 to 1.5 times the theoretical oxygen quantity necessary for decomposing the ammonia, org. material and inorg. material in the treated liquid.

Description

DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to a method for treating wastewater and sludge, and more specifically, the present invention relates to a method for treating wastewater and sludge. This invention relates to a method for simultaneously treating sludge derived from wastewater.

BACKGROUND OF THE INVENTION PRIOR ART AND THEIR PROBLEMS Recently, with the improvement of living standards, especially dietary standards, the amount of kitchen waste, along with other household waste, has increased significantly. Currently, kitchen waste is collected as so-called raw garbage along with other household garbage and disposed of in landfills or incinerated.

However, since kitchen waste is characterized by extremely high water content, its disposal poses various problems. For example, it may cause environmental pollution problems when stored in homes, apartment complexes, buildings, etc., it may be complicated to transport, it may become a source of bad odors due to rotting in landfills, and it may become a source of sanitary pests such as flies. or it may be difficult to incinerate. In addition, kitchen waste, due to its high water content, is also one of the factors that prevents an increase in the amount of energy recovered by incineration.

Attempts have been made to separately collect (and compost) raw garbage, but seasonal qualitative changes (for example, intensive disposal of watermelon peels with extremely high water content in summer) and public interest in separate collection It has not been widely used due to problems such as low yield and unstable marketability as compost.

Therefore, effective treatment of kitchen waste requires storage,
It is one of the important issues in waste treatment technology in many aspects such as collection, transportation, and incineration.

As a method for disposing of kitchen waste, there is also a method of crushing it with a disposer, discharging it into the sewer along with the wastewater, and disposing of it along with the sewage, as is done in Europe and the United States. 15
However, in Japan, such treatment methods are rather discouraged from the viewpoint of increasing the load on existing wastewater treatment facilities and preserving water quality9.

In Ichiriki, the treatment of large amounts of sludge generated from sewage treatment plants is already a serious problem.
There is a strong desire to establish technology for economically processing kitchen waste, sewage, and sludge.

Means for Solving the Problems As a result of intensive research in view of the problems listed in Section L regarding the processing of kitchen waste, the inventor has developed a method for processing kitchen waste that has been crushed and turned into sludge by a disposer. After discharging along with the waste water into a dedicated drain pipe connected to the sewer or wastewater treatment facility,
If the solids and liquid components in the mixture are separated and the solids and liquid components are treated separately prior to treatment at a sewage treatment plant or wastewater treatment facility, the load on the wastewater treatment facility will increase. It has been found that various problems in waste disposal caused by kitchen waste can be alleviated while avoiding situations such as deterioration of water quality17.

In particular, it has been found that excellent economical results can be obtained by subjecting the solid matter separated in [2] and sludge from a sewage treatment plant together to wet oxidation treatment as described above.

That is, the present invention provides the following methods for treating wastewater and sludge: (1) A method for treating wastewater and sludge, which comprises: (1) crushing kitchen waste into slurry and turning it into domestic wastewater and/or industrial wastewater; (2) Separation of solids and liquid components in the mixture prior to treatment at a sewage treatment plant or wastewater treatment facility. (3) A step of treating the liquid component separated in (2) above with activated sludge; (4) A step of treating the liquid component separated in (2) above with activated sludge; (5) mixing the mixture obtained in (4) above with sewage or wastewater in the presence of oxygen;
H about 1 to 11.5, a step of wet oxidative decomposition at a temperature of 100 to 370°C, and (6) a honeycomb-shaped supported catalyst containing at least one of a noble metal and a base metal as an active ingredient in the treatment liquid obtained in (5) above. The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the treatment liquid in the presence of 1 to 1.
pH approximately 1-11,5, temperature 10 in the presence of 5 times the amount of oxygen
A method for treating wastewater and 7"ffi&, comprising a step of wet oxidative decomposition at 0 to 370°C.

■ A method for treating wastewater and sludge, which includes (1) a process of pulverizing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and discharging the mixture into a sewer or a dedicated drain pipe connected to wastewater treatment equipment; (2) Prior to treatment at a sewage treatment plant or wastewater treatment facility, the solids and liquid components in the mixture are separated; (3) the liquid component separated in (2) above is treated with activated sludge. (4) A step of mixing the solids separated in (2) above and the solids generated or recovered in a sewage treatment plant or wastewater treatment facility into sewage or wastewater, (5) Item th (4) ) wet oxidation of the mixture obtained in step (5) above in the presence of oxygen at a pH of approximately 1 to 11.5 and a temperature of 100 to 370°C; The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the treatment liquid in the presence of a honeycomb-shaped supported catalyst containing one type of active ingredient.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
A method for treating wastewater and sludge, comprising a step of performing wet oxidative decomposition at 0 to 370°C, and (7) a step of performing anaerobic methane fermentation treatment on the treated liquid obtained in (6) above.

■ A method for treating wastewater and sludge, which involves (1) crushing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and discharging the mixture into a sewer or a dedicated drainage pipe connected to wastewater treatment equipment. (2) a step of separating solids and liquid components in the mixture prior to treatment at a sewage treatment plant or wastewater treatment facility; (3) converting the liquid component separated in (2) above into activated sludge; (4) A step of mixing the solids separated in Section F (2) with the solids generated or recovered in a sewage treatment plant or wastewater treatment facility into sewage or wastewater; (5) The above The mixture obtained in (4) was heated to p in the presence of oxygen.
(6) Wet oxidative decomposition step at a temperature of about 1 to 11□5 and a temperature of ioo to 370°C. The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the presence and in the treatment liquid is 1 to 1.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
A step of wet oxidation decomposition at 0 to 870°C, (7) a step of treating the treated liquid obtained in (6) above with activated sludge under normal pressure or pressurization, and (8) a surplus from (7). A method for treating wastewater and sludge, comprising a step of returning the sludge to the above (5).

■ A method for treating wastewater and sludge, which includes (1) a process of pulverizing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and discharging the mixture into a sewer or a dedicated drain pipe connected to wastewater treatment equipment; (2) A step of separating solids and liquid components in the mixture prior to treatment at a sewage treatment plant or treatment at a wastewater treatment facility; (4) A step of mixing the solids separated in (2) above with the solids generated or recovered in a sewage treatment plant or wastewater treatment facility with sewage, (5) (4) above. wet oxidative decomposition of the mixture obtained in the presence of oxygen at a pH of approximately 1 to 11.5 and a temperature of 100 to 370°C; The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the treatment liquid in the presence of a honeycomb-shaped supported catalyst containing one type of active ingredient.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
wet oxidative decomposition at 0 to 370°C; (7) anaerobic methane fermentation treatment of the treated liquid obtained in (6) above; (8) activated sludge treatment of the treated liquid obtained in (7) above. and (9) a step of returning surplus sludge from (7) and/or (8) to (5).

In the following, the inventions shown in the above sections (1) to (2) will be referred to as the first method to the fourth method of the present application, respectively, and each will be explained in detail with reference to the accompanying drawings.

■1 First method of the present application As shown in Figure 1, in the first method of the present application, first,
After pulverizing kitchen waste (1) generated at homes, restaurants, etc. into a slurry (as pulverized material, 5C1 or less, more preferably 1 mm or less) using a disposer (3),
Solid content (
(hereinafter referred to as SS) is sent to a separator (11). The liquid components separated here are sent to an activated sludge tank (13) and subjected to activated sludge treatment according to a conventional method. However, from the liquid component,
Since the ss is separated in advance, the capacity of the activated sludge tank (13) can be reduced by 2 compared to the conventional one. The solid content (15) formed in the SS separator (11) and the excess sludge (J, 7) from the activated sludge tank (13) are sent to the sludge thickener (19) and concentrated.

The method shown in FIG. 1 is suitable for implementation in areas without sewage systems or in wastewater treatment facilities other than sewage treatment plants (for example, wastewater treatment facilities attached to factories).

In the method shown in Fig. 2, kitchen waste (1) is crushed by a disposer (3) and then combined with domestic wastewater (5) and industrial wastewater (7) containing human waste, septic tank sludge, etc. flow to. After separating coarse solids, sand, etc. from the mixed liquid by sedimentation in the initial settling tank (23), S
SS in the wastewater is recovered in the S separator (11). S
The liquid component not containing S is sent to the activated sludge tank (13),
Treat with activated sludge according to conventional methods. In this case as well, SS is separated from the liquid components, so the activated sludge tank (
The capacity of 13) can be made smaller than that of the conventional one. Next, the liquid component is sent to the final settling tank (25),
Perform sedimentation separation. 5S (27), 5S (15), excess sludge (29) from activated sludge tank (13) and final settling tank (
5S (31) from 25) is collected in a sludge thickener (technique 9) and concentrated.

The method shown in Figure 2 is suitable for implementation in areas with sewerage infrastructure.

The thickened sludge (moisture content 90% or more) obtained in the treatment process shown in Figure 1 or Figure 2 is sent to the wastewater/sludge storage tank (101) as shown in Figure 3, where it is mixed. After that, it is pumped through the line (105) by the pump (103), and the pressure is increased by the compressor (107) and the line (
After being mixed with oxygen-containing gas pumped from 109),
It reaches the line (115) via the line (ill') and the heat exchanger (113).

When the thickened sludge reaches a predetermined temperature or higher due to heat exchange in the heat exchanger (113), the thickened sludge is transferred to the line (117).
and (1, 19) to the first reaction zone (121), and if the predetermined temperature has not been reached, the line (
123), a heating furnace (125>), a line (127) and a line (119) are fed to the first reaction zone (121). 11.5, more preferably about 3 to 9, an alkaline substance or an acidic substance, usually in the form of an aqueous solution, is added to the line (13) from the pH regulating material storage tank (129).
1), pump (133), line (135) and line (137). Also, line (13
The concentrated sludge may be sent to a pH-adjusting material water/sludge storage tank (lot) via a line (132') branching from 1) to adjust the pH of the concentrated sludge in advance. First reaction zone (12
In 1), liquid phase oxidation of thickened sludge is carried out in the presence of oxygen-containing gas without the use of catalysts. The oxygen-containing gas used includes air, oxygen-enriched gas, oxygen, and one or more of hydrogen cyanide, hydrogen sulfide, ammonia, sulfur oxides, organic sulfur compounds, nitrogen oxides, hydrocarbons, etc. Examples include oxygen-containing waste gas. The supply amount of these gases is 1 to 1.5% of the theoretical amount of oxygen required to oxidize and decompose SS, organic components (COD components), ammonia, etc. in the thickened sludge into nitrogen, carbon dioxide, water, etc.
It is preferable to supply 5 times the amount of oxygen, more preferably 1.05 to 1.2 times the amount of oxygen.

When oxygen-containing waste gas is used as the oxygen source, there is an advantage that harmful components in the gas can also be treated at the same time. If the absolute amount of oxygen is insufficient when using oxygen-containing waste gas, it is preferable to compensate for the deficiency with air, oxygen-enriched air, or oxygen.

Note that it is not necessary to supply the entire amount of oxygen-containing gas to the thickened sludge supplied to the main wet oxidation process as the first reaction zone; It may be distributed and supplied. For example, in the present wet oxidation step as the first reaction zone, S
About 10 to 90% of S is decomposed or solubilized, about 10 to 60% of COD components, and about 0 to 15% of ammonia are decomposed, so the amount of oxygen is 0.4 to 0.8 times the theoretical amount of oxygen. A corresponding amount of oxygen-containing gas may be supplied, and the remainder may be supplied as a second reaction zone in the next step as 2. The temperature during the reaction in this wet oxidation step as the first reaction zone is:
Usually 100-370℃, more preferably 200-300℃
It is about ℃.

The higher the temperature during the reaction, the higher the partial pressure of oxygen in the supplied gas, and the higher the operating pressure, the higher the decomposition rate of the components to be treated that also solubilizes SS. Although the residence time of the thickened sludge in the reactor is shortened and the reaction conditions in the next process are eased, on the other hand, the equipment cost increases, so it is important to consider the type of thickened sludge, the balance with the reaction conditions in the next process, and the requirements. It may be determined by comprehensively considering the extent of processing to be performed, overall operating costs, equipment costs, etc. The pressure during the reaction may be at least the minimum pressure at which the thickened sludge maintains a liquid phase at a predetermined reaction temperature. The reaction time may vary depending on the size of the reactor, water quality of the thickened sludge, temperature, pressure, etc., but is usually 15
It is about 120 minutes, preferably about 30 to 60 minutes.

Next, in the first method of the present application, the first reaction zone (121
) is transferred to a second reaction zone (139
), where it is again subjected to liquid phase oxidation. The structure of the honeycomb-shaped carrier may be one in which the openings have any shape such as square, hexagonal, or circular. Area per unit capacity,
Although the aperture ratio is not particularly limited, it is usually used that has an area per unit capacity of about 200 to 800 m2/m" and an aperture ratio of about 40 to 80%. Materials for the honeycomb structure include titania, Examples include zirconia. As the catalyst active component, at least one of noble metals and base metals is used. Examples of the noble metal catalyst active component include ruthenium, rhodium, palladium, osmium, iridium, platinum, gold, etc. Base metal catalyst active components include iron, copper, cobalt, manganese, nickel, magnesium, tungsten, etc.If necessary, these catalyst active components include tellurium, lanthanum, cerium, selenium, etc. By using the co-catalyst component in combination, it is possible to increase the activity of the catalytic active component and improve the heat resistance, durability, and mechanical strength of the catalyst body. ,
The amount of catalyst active component supported is usually 0.05 to 2 of the carrier weight.
It is about 5%, preferably about 0.5 to 3%. Also,
The amount of co-catalyst component used is 0.01 based on the catalytic active component.
It is about 30%. In the case of a fixed bed, the reaction column volume is such that the space velocity of the liquid is 0.5 to 10'/hr (based on the empty column),
More preferably, it is 1 to 4'/hr (empty tower standard).

The temperature and pressure conditions during the reaction in the second reaction zone (139) may be the same as those in the first reaction zone (121,).

The treated water from the first reaction zone (121) may be supplied with oxygen-containing gas from the compressor (107) via the line (141'), and the pHXm adjustment material storage tank (129
) to the line (131) and the pump (1
33), may be added to the lower part of the second reaction zone (139) via line (135) and line (143).

Note that the alkaline substance is placed at appropriate positions (not shown) in the first reaction zone (121) and the second reaction zone (139).
It may be supplied to

The high temperature treated water subjected to liquid phase oxidation in the second reaction zone (139) passes through the line (145) to the heat exchanger (11).
3), where the untreated thickened sludge is given thermal energy and then enters the cooler (149) via line (147) where it is cooled. Further, if necessary, high temperature treated water may be introduced into a wastewater/sludge storage tank (101) (not shown) and the concentrated sludge may be preheated by heat exchange. This preheating greatly reduces the viscosity of the thickened sludge, making it easier to treat it. If the temperature of the cooling water from the line (147) is around 50℃, the cooler (14, 9)
There is no need to use . The treated water that has exited the cooler (149) passes through a line (151) and is separated into a gas from a line (155) and a liquid from a line (157) in a gas-liquid separator (153). Second reaction zone (139)
If the treated water obtained in step 2 contains nonflammable ash, a separation membrane, gravity sedimentation separation tank, etc. (not shown) may be provided in line (157) J2 to remove the ash.

Depending on the degree of cleanliness, the liquid from the line (157) can be used as gray water, directly discharged into a river, etc., returned to the activated sludge tank (13) for further treatment, or It is returned to the wastewater/sludge storage tank (101) for further treatment.

(1) First Method of the Present Application The processing of kitchen waste in the second method of the present application may be carried out in accordance with the flow shown in FIG. 1 or FIG. 2 in the same manner as the first method of the present application.

Furthermore, the treatment of thickened sludge in the third method of the present application is carried out in substantially the same manner as in the first method of the present application. However, in the second method of the present application, as shown in FIG.
The warm liquid component from the anaerobic methane fermenter (
After being sent to line (159') and subjected to economically advantageous digestion treatment under efficient high temperature conditions, the treated water is removed from line (161'). The conditions for anaerobic methane fermentation are not particularly limited, but the usual temperature is about 35 to 60°C, and the number of days for digestion is 0.
．． For about 5 to 30 days, the sludge concentration is about 0.5 to 5%.

Excess sludge produced in the anaerobic methane fermentor (159) is mixed with wastewater on the line (105), for example, and returned to the first reaction zone (121), where it is treated together with the thickened sludge.

Furthermore, the treated liquid from the anaerobic methane fermentation tank (159) can be used as gray water, directly discharged into a river, or returned to the activated sludge tank (13) or the wastewater/sludge tank (101).

(1) 0 First Method of the Present Application The processing of kitchen waste in the third method of the present application may be carried out in accordance with the flow shown in FIG. 1 or FIG. 2 in the same manner as the first method of the present application.

Further, the treatment of thickened sludge in the third method of the present application is carried out in substantially the same manner as the second method of the present application, except for the treatment at the final stage. That is, in the flow shown in Fig. 4, by providing an aerobic treatment tank (1B2) using the activated sludge method in place of the anaerobic methane fermentation tank (159') (see Fig. 5), the water from the line (157) is The liquid component can be treated. In this case, the gas from the line (155) is pressure-adjusted and then supplied to the aerobic treatment tank (162) and used as at least a part of the oxygen source under normal pressure or under pressure. Excess sludge generated in the aerobic treatment tank (1B2>) is also returned to the first reaction zone (121') and treated together with the thickened sludge.

In addition, the treated liquid from the aerobic treatment tank (162) can be used as gray water, directly discharged into rivers, or activated sludge tank (162)
3) or can be returned to the wastewater/sludge tank (101).

(1) First Method of the Present Application The processing of kitchen waste in the fourth method of the present application may be carried out in accordance with the flow shown in FIG. 1 or FIG. 2 in the same manner as the first method of the present application.

Furthermore, the treatment of thickened sludge in the fourth method of the present application is carried out in substantially the same manner as the first method of the present application, except for the treatment at the final stage. That is, as shown in FIG.
) is first treated in an anaerobic methane fermentation tank (159), and then sent through a line (161) to an aerobic treatment tank (1B2) using an activated sludge method for activated sludge treatment.

In addition, in the apparatus shown in FIG. 6, a gas-liquid separator (153) is provided following the second reaction zone (139''), and gas components are passed through the line (177) and the heat exchanger (
113) and line (181), and if necessary, after cooling and pressure adjustment (not shown), the aerobic treatment tank (
Activated sludge treatment is carried out under normal pressure or pressurization. On the other hand, the liquid component from the gas-liquid separator (153') is supplied to the line (179'), the heat exchanger (1
65), line (183), cooler (149') and line (185) into the anaerobic methane fermentation tank (159), and then sent to the aerobic treatment tank (182').

Methane fermentation layer (159) and aerobic treatment tank (1B2)
The surplus sludge produced in is also returned to the second reaction zone (121) and treated together with the thickened sludge.

In addition, the treated liquid from the aerobic treatment tank (1B2) can be used as gray water, directly discharged into rivers, or activated sludge tank (1B2).
13) or can be returned to the wastewater/sludge tank (LOI).

According to the present invention, the following effects are achieved in garbage treatment and wastewater treatment.

(1) By crushing kitchen waste into slurry using a deposer,
Garbage can be disposed of hygienically, economically and efficiently. More specifically, the following results can be obtained.

(a) Cleanliness is ensured in the kitchen and its surroundings.

(b) Housework and kitchen work are reduced.

(e) Maintaining cleanliness and preventing bad odors during garbage collection is achieved, making collection work easier.

(d) The amount of garbage collected and transported will decrease.

(e) The amount of energy recovered at waste incineration plants will increase.

(f) Secondary pollution generated when garbage is landfilled is reduced.

(2) Furthermore, since the wastewater is treated after separating and collecting the crushed kitchen waste and SS in the wastewater, unlike the conventional technology in which wastewater is treated in a state containing SS, solubilized Since the wastewater BOD and COD components are treated, even with the introduction of a disposer, problems such as increased load on wastewater treatment equipment and deterioration of water quality do not occur.

For example, when processing at a sewage treatment plant, the aeration capacity of conventional aerobic treatment is 6 times higher than the amount of sewage water flowing, according to the standards of the Ministry of Construction.
In contrast, when the crushed slurry of kitchen waste and the SS in the wastewater are treated together with the surplus sludge produced by the method of the present invention, the treatment time is reduced to about 1/3.
It can be shortened to a certain extent.

(3) In addition, by simultaneously treating suspended matter containing crushed kitchen waste separated from wastewater and surplus sludge from the wastewater treatment system, not only ammonia and COD components but also suspended components can be efficiently treated. can do.

That is, in the present invention, without the need for a sludge dewatering process, the first stage of oxidation of the thickened sludge is carried out in the liquid phase in the absence of a catalyst and in the presence of an oxygen-containing gas. Solubilization of SS proceeds. Next, nitrogen-containing oxides such as ammonia are decomposed by a second stage liquid phase oxidation carried out in the presence of a catalyst and in the presence of oxygen, and COD components including SS components are also decomposed depending on the selection of reaction conditions. At the same time as being completely or partially decomposed, most of the polymeric substances are converted into lower aliphatic carboxylic acids such as acetic acid by the action of a catalyst. and,
The low molecular weight biologically easily degradable products in the liquid to be treated that have been subjected to the liquid phase oxidative decomposition treatment as described above are very efficiently decomposed by anaerobic methane fermentation treatment and/or aerobic treatment.

Therefore, by introducing a disposer, even if the amount of pollutant components in wastewater increases temporarily, the wastewater can be effectively treated without increasing the load on the wastewater treatment equipment itself.

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

Reference example 1 For the purpose of understanding the amount of kitchen waste generated and its composition, 5
Two days worth of kitchen waste from 0 households was collected and analyzed. For the analysis, the entire kitchen waste was prepared by the quartering method and divided into a sample for compositional analysis and a sample for disposer processing, and then analyzed.

Samples for disposer processing are made by continuously charging and crushing 1 kg of kitchen waste, adding tap water to this, and adjusting the liquid volume to IOQ.
And so. Next, the load amount per 100 g of kitchen waste was determined from the concentration of the liquid. The results are shown in Table 1. In addition, the particle size distribution of the crushed mud is less than 0.15 mm = 47%, 0.15
~1wim=40%, 1-5mm-remainder.

In addition, from the results of the analysis, it is estimated that the average amount of kitchen waste generated per person per day is 240g, and based on this, 1
The daily load per person was determined.

The results are shown in Table 2.

In addition, in each table below, "T-N" means the total nitrogen amount.

Table 1 BOD CODM, SS TN Maximum (g) 14.0 8°25 18.5
0.94 average (g) 9.5 B, 3
12.4 0.77 minimum (f) 6.6 4.
0 0.45 0.55 Table 2 BOD CODM, SS T N Maximum (g) 33.6 19.8 44.4
2.26 average (g) 22.8 15.1
29.8 1.85 minimum (g) 1B, 6 9
．． 6 10.8 1J2 Based on the above results, 2 per day
The load amount per 50,000 people was calculated. The results are shown in Table 3.

Furthermore, the increase in the amount of sewage water per 250,000 people per day due to the use of deposers is approximately 4%, or approximately 5,000 m3 (191 m3).
2/person/day).

Table 3 BOD CODM-SS T N Maximum (g) 8400 4950 11100 5
65 average (g) 5700 3775 7450
462.5 minimum (g) 4150 2400 2
700 330 Furthermore, using the average values in Tables 1 to 3 above, calculate the concentration of each component before and after the use of a disposer in an existing final sewage treatment plant (250,000 people: 1125,000 m3/day of sewage treatment). Table 4 shows the results of trial calculations regarding the load conditions.

Table 4 Before using disposer After using Increase rate (%) Concentration (mg/R) BOD 140 179
27.9 CODM,, 87 113 29.9
SS 125 178
42.4T-N 27
29.6 9.6 Load (lie/day) B OD 17430 23130
32.7COD Mo10830 14605
34, 9S S 20000 2
7500 37.8T-N 338
0 3823 13.8 Note: SS includes sludge produced in biological treatment tanks.

It is predicted that the load will increase by about 38% for SS and about 15% for total nitrogen components.

Example 1 According to the flow shown in FIG. 2, the suspension collected from the initial settling tank (23) and the final settling tank (25) and the activation treatment tank (
To 1 part of the mixture of surplus sludge from 13), 0.38 parts of sludge obtained by crushing kitchen waste with a deposer (both dry weight) was added, and the mixture was combined with sewage to form a sewage sludge concentrate as follows. It was subjected to processing.

The composition and properties of the sewage sludge concentrate are as follows.

From the results shown in Table 4, by using a disposer,
BOD and CODM, about 30-35% Table 5 pH 6,7 CODM-(+g/R) 18000COD
c= (mg/Q) 3800ON H3N
(mg/Q) 600T-N
(mg/R) 3200BOD (■
g/Q) 13000SS (ag/Q
) 40000VSS (ig/Q)
28000TOD (-g/Q)
64,000 TOC (g/ (2)
1 3 3 0 0 then,
The sewage sludge concentrate with the composition shown in Table 5 was prepared at a space velocity of 1.01.
/Hr (sky column basis) and mass velocity 7,96 t/
The reaction zone (1
21). On the other hand, space velocity 2271/H
Air was supplied to the lower part of the first reaction zone (121) at r (empty column basis, standard state conversion). In this state the temperature is 250
The wastewater was subjected to non-catalytic liquid phase oxidation treatment under the conditions of temperature and pressure of 90 kg/cI12.G.

Table 6 shows the composition of the treated water obtained in this step.

Table 6 pH6.3 COD+, +1 (+wg#) 2000CODc-(
Ig/Q) 1079ONH3-N (mg/R)
2500 TN (rg/g) 2770 BOD (+ag/Q) 9555 S S (mg/Q) 12280 VSS (ig/R) 280 TOD (mg/Ω) 20800 TOC (mg/Q) 4320 Table 5 and As is clear from the comparison with Table 6, the non-axial [, phase oxidation! ,1:J,6CODM,,COD,,,,TO
The decomposition rates of D and TOC were 88.9% and 71.9%, respectively.
6%, 67.5% and 67.5%.

Furthermore, since the nitrogen-containing compounds were converted to ammonia, the ammonia concentration was approximately four times higher.

Next, the opening shape is a square (-side length 3.5-m), and the cell pitch is 4. 5mm, Kaikouri 59.3
% titanium honeycomb carrier supported with 2% of the carrier weight of ruthenium, the honeycomb catalyst body was packed so that the amount was 3/4 of the empty column volume in the previous step (45 minutes as reaction time in the catalyst bed). The treated water and air from the non-catalytic wet oxidation step were supplied to the second reaction zone (139), where liquid phase oxidation was performed. The reaction temperature was 270°C, and the pressure was the same as in the non-catalytic wet oxidation process.

Table 7 shows the composition of the treated water obtained in this step.

Table 7 pH 3, O CODM, (weight g/l') 4
12CODc-(mg/R) 4824N
H3-N (mg/Q) 26T-N(
mg/F) 65BOD (mg/
Q) 2207SS (mg/9)
8410VSS (Ig#)
95TOD (wg/R) 665
6TOC (mg/R), 1630 As is clear from the comparison between Tables 5 and 7, C0Dc, and TO
The amount of decomposition of D per wastewater IQ is 33176 mg each.
and 57344 mg.

The reaction could be carried out without external heat supply due to the reaction heat due to the decomposition of these components and the reaction heat due to the decomposition of the ammonia component. That is, in the flow shown in FIG. 3, there was no need to use the heating furnace (125).

Example 2 After treating the sewage sludge concentrate in the same manner as in Example 1, the treated water from the catalytic wet oxidation process was transferred to a heat exchanger (l13
) and a cooler (149), and was further sent to a gas-liquid separator (153) to separate it into exhaust gas and treated water. The temperature of the treated water was adjusted using a cooler (149) so that the temperature in the anaerobic methane fermentation tank in the next step was about 55°C.

The exhaust gas from the gas-liquid separator (153) contains NH3,
SOX and NOx were not detected.

The treated water from the above process was then led to a gravity sedimentation separation tank (not shown) to separate and remove residual SS.

More than 99% of the separated SS was noncombustible ash.

After adjusting the pH of the liquid from the gravity sedimentation tank to approximately 7.5 with a 10% sodium hydroxide solution, it was transferred to an anaerobic methane fermentation tank (
159). The anaerobic methane fermentation tank was of a fluidized bed type, and microbial cells were attached to porous ceramic particles having a particle size of 300 μm, and a fluidized bed was formed using a circulation pump.

Table 8 shows the water quality of the digestive fluid after anaerobic digestion (results of the second method of the present invention, which corresponds to FIG. 4).

The surplus sludge after anaerobic digestion was returned to the first non-catalytic wet oxidation process for treatment.

Table 8 pH 7, I CODM,, (ff1g#) 46CODc, (l
l1g/R) 48ONH3N (mg/Q) 12 TN (mg/ff) 25 BOD (mg/Q) 220 SS (D/R) 45 TOC (mg/&) 163 Example 3 Obtained in Example 2 treated water (SS has been separated and removed, approx.
5°C) was further aerobically treated using the activated sludge method.

Table 9 shows the water quality after aerobic treatment (results of the fourth method of the present invention, which corresponds to FIG. 6).

Table 9 pH7, O CODMn (mg/Q) 5NH3
-N (1g/Q) 8T
-N (Otori g/Q)
1 0BOD (-g/Q)
9SS (mg/Q)
ITOC (wear g/Q)
9. The excess sludge after the aerobic treatment was returned to the first non-catalytic wet oxidation step for treatment.

Examples 4 to 7 The same sewage sludge concentrate as in Example 1 was subjected to non-catalytic wet oxidation treatment in the same manner as in Example 1, and then the same procedure as in Example 1 was carried out except that the reaction time was changed as shown in Table No. The treated solution was further subjected to catalytic wet oxidation treatment in the same manner as above.

The results are shown in Table 10.

Table 10 Reaction time (min) COD M-(ig/Q) COD c= (mg/Q) NH3N (I1g/Q) TN(mg/ff) BOD(D/Q) SS (II1g/Q ) VSS (mg/Q) TOD (mg/Q) IOC (Ig/Q) ] 5 1F0 Not detected 15.9 Not detected 9.3 1.85 Examples 8 to 11 Sewage sludge similar to Example] The space velocity of the concentrate is 2, 0
Non-catalytic wet oxidation treatment was carried out in the same manner as in Example 1 except that the oxidation rate was 1/hr.

The results of the treated solution obtained by this non-catalytic wet oxidation are
It is shown as (I) in Table 1.

Next, the treatment liquid from the non-catalytic wet oxidation treatment step was further subjected to a catalytic wet oxidation treatment in the same manner as in Example 1, except that the reaction time was changed as shown in Table 11.

The results are shown in Table 1.

Reaction time (min) CODM. (mg#riCOD c-(mg/R) NHI-N (D/Q T-N (mg/Q) BOD (og/r2) 55 (mg/9) VSS (B/Q) TOD (mg/Q) ) TOC (mg/Q) E1 ] 1.4300 3300 Table 18 Undetected Undetected Example 12 The same sewage sludge concentrate as in Example 1 was subjected to non-catalytic wet oxidation treatment in the same manner as in Example 1.

Next, the treatment liquid from the non-catalytic wet oxidation treatment step was further subjected to a catalytic wet oxidation treatment in the same manner as in Example 2.

Next, the treatment liquid from the catalytic wet oxidation treatment step is passed through the fifth
Follow the flow shown in the figure to activate the activated sludge treatment tank (1B2
) was subjected to aerobic treatment. Aerobic treatment was carried out at 35℃, 2
kg/cd, and the gas necessary for aeration was the exhaust gas from the catalytic wet oxidation treatment step, which was pressure-controlled.

Table 12 shows the water quality after aerobic treatment (results of the third method of the present application).

Table 12 pH7.2 COD Mo (mg/Q)
8NH3N (mg/Q) 9T
-N (-g/Q) 11BOD(
mg/R) 12SS (■g/
Q) ITOC (mg/g”)
10 Examples] 3 (a) A sewage sludge concentrate having the same composition as in Example 1 was subjected to non-catalytic wet oxidation treatment in the same manner as in Example 1 except that the temperature was 260°C and the pressure was 95 kg/cd-G. .

(b) Next, the treatment liquid from the non-catalytic wet oxidation treatment step was further subjected to a catalytic wet oxidation treatment in the same manner as in Example 1 except that the temperature was 280° C. and the pressure was 95 kg/cd·G.

(C) Next, the pH of the treatment liquid from the catalyst wet oxidation treatment step was adjusted to 6.8 with a sodium hydroxide solution, and filtered using an ultrafiltration membrane to separate and remove SS.
Follow the flow shown in the figure to activate the activated sludge treatment tank (1B2
) was subjected to aerobic treatment. Aerobic treatment at 35℃
, 2 kg/e-, and the exhaust gas from the catalyst wet oxidation process was used as the gas necessary for aeration by controlling the pressure.

Since 99% of the separated SS was nonflammable ash, it was taken out of the system.

Table 13 shows the water quality after each step.

Table H COD M-(mg/Q) NHI-N(mg/Q T-N(mg/RBOD)(1g/Q SS(D/R VSS(mg/Q TOD(layer g/Q TOC(mg/ (2 6,5 2,1 6,8 In addition, in the exhaust from the gas-liquid separator (153), NH3
, SOx and NOx were not detected.

Furthermore, even after 6,000 hours of processing the same sewage sludge concentrate as in Example 1 containing a high concentration of SS, no decrease in the decomposition rate of each component was observed in each step, and the wastewater treatment continued. I was able to do it without any problems.

Examples 14 to 26 The same sewage sludge concentrate as in Example 1 was treated by the third method of the present application according to the flow shown in FIG.

The liquid hourly space velocity in the non-catalytic wet oxidation process and the catalytic wet oxidation process is 1. 01/Hr (empty column basis) and 0.671/Hr (empty column basis).

The honeycomb-shaped catalyst used in the catalytic wet oxidation process was
As shown in the table.

Conditions other than the above were the same as in Example 1.

Table 14 shows the quality of the treated water obtained in the catalytic wet oxidation step and the aerobic sludge treatment step.

Table Example 27 and Comparative Examples 1 to 2 Treated samples were prepared by adding crushed kitchen waste to sewage so as to correspond to the water quality of the sewage after use of the disposer shown in Table 4 above.

After separating the SS component from the treated sample thus prepared, aerobic treatment was performed using an activated sludge method under conditions of a temperature of 35° C. and a residence time of 2 hours.

Further, the SS component was subjected to a two-stage wet oxidation treatment in the same manner as in Example 1, and similar results were obtained.

In addition, for comparison, without separating the SS component, directly under the conditions of a temperature of 35 ° C. and a residence time of 2 hours (comparative example) -
), or directly under the conditions of a temperature of 35° C. and a residence time of 8 hours (Comparative Example 2). Aerobic treatment was performed by an activated sludge method.

The results of aerobic treatment are shown in Table 5.

Table 15 Sample Example Comparison Comparative water quality 27 Example 1 Example 2 SS (a+g/Q> 178 < 1 1
2.1 8.9BOD c/Q> 179
7 18.0 10.5T-N (D/R) 2
9.6 13 16.7 1B,5CODM-(mg
/R) 113 8 15.0 11.0 Example 28 Each treated water from the catalytic wet oxidation process of Examples 1 to 3 and Examples 4 to 7 was transferred to the biological treatment tank of the original sewage treatment system shown in FIG. (13) for aerobic sludge treatment (normal pressure,
The temperature was 35°C and the residence time was 2 hours). The return amount is
It was 0.53% with respect to the sewage outlet.

The quality of each water after aerobic treatment was within the range shown in Table 16.

Table 16 SS (mg/R) 1-5 BOD (ig/Q) 7-15 TN (mg/Ω) 7-18 CODMn (Ig/Q) 4-17 Reference Example 2 Results of the Example of the present application For reference, we calculated the energy balance when kitchen waste and sewage were treated by the method of the present invention per 250,000 people per day, and the results shown in Table 17 were obtained. The results according to the current situation are shown as (I), the results according to the method of the present invention are shown as (n) and 2, and the difference between the two is shown as (m
).

The results shown in Table 17 are expressed in gigacalories over 7 years.

In Table 17, the numbers with Δ represent the energy consumed for treatment, and the numbers with 10 represent the recovered energy obtained by the treatment.

From the results shown in Table 17, it is clear that the method of the present invention achieves significant overall energy savings.

[Brief explanation of drawings]

1 to 6 are flowcharts illustrating embodiments of the present invention. (1)...Kitchen waste (3)...Disposer (5)...Domestic wastewater (7)...Industrial wastewater (9)...Special drain pipe (11)...SS separator ( 13)...Activated sludge tank (15)...SS (17)...Excess sludge (19)...Sludge thickener (21)...Sewerage (23)...Initial settling tank (25) )...Final settling tank (27)...5S (29)...Excess sludge (31)...5S (101)...Wastewater/sludge storage tank (103)...Pump (107) ... Compressor (113) ... Heat exchanger (121'') ... First reaction zone (125') ... Heating furnace (129) ... pH adjusting substance storage tank (133) ... Pump (139)... Second reaction zone (149>... Cooler (153)... Gas-liquid separator 059)... Anaerobic methane fermentation tank (162)... Aerobic treatment tank ( 2)

Claims (1)

[Claims] [1] A method for treating wastewater and sludge, which comprises: (1) crushing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and conveying the mixture to a sewer or wastewater treatment facility; (2) a step of separating the solids and liquid components in the above mixture prior to treatment at a sewage treatment plant or wastewater treatment facility; (3) a step of discharging the solids and liquid components in the above mixture into a dedicated drainage pipe; (4) A step of mixing the solids separated in (2) above with solids generated or recovered in a sewage treatment plant or wastewater treatment facility into sewage or wastewater. , and (5) the mixture obtained in (4) above in the presence of oxygen.
H about 1 to 11.5, a step of wet oxidative decomposition at a temperature of 100 to 370°C, and (6) a honeycomb-shaped supported catalyst containing at least one of a noble metal and a base metal as an active ingredient in the treatment liquid obtained in (5) above. The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the treatment liquid in the presence of 1 to 1.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
A method for treating wastewater and sludge, comprising a step of wet oxidative decomposition at 0 to 370°C. [2] A method for treating wastewater and sludge, comprising: (1) crushing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and discharging the mixture into a sewer or a dedicated drain pipe connected to wastewater treatment equipment; step, (2) separating the solids and liquid components in the mixture prior to treatment in a sewage treatment plant or wastewater treatment facility, (3) treating the liquid component separated in (2) above with activated sludge treatment. (4) A step of mixing the solids separated in (2) above and the solids generated or recovered in a sewage treatment plant or wastewater treatment facility with sewage or wastewater, (5) (4) above. The mixture obtained was heated to p in the presence of oxygen.
(6) Wet oxidative decomposition step at a temperature of 100 to 370° C. at a temperature of 100 to 370°C; The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the presence and in the treatment liquid is 1 to 1.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
wet oxidative decomposition at 0 to 370°C, (7) anaerobic methane fermentation treatment of the treated liquid obtained in (6) above, and (8) excess sludge from (7) above to (5) above. A method for treating wastewater and sludge, characterized by comprising a return process. [3] A method for treating wastewater and sludge, comprising: (1) Pulverizing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and discharging the mixture into a sewer or a dedicated drain pipe connected to wastewater treatment equipment. (2) a step of separating solids and liquid components in the mixture prior to treatment at a sewage treatment plant or wastewater treatment facility; (3) converting the liquid component separated in (2) above into activated sludge; (4) A step of mixing the solids separated in (2) above with the solids generated or recovered in a sewage treatment plant or wastewater treatment facility into sewage or wastewater; (5) The above ( The mixture obtained in step 4) was heated to p in the presence of oxygen.
(6) Wet oxidative decomposition step at a temperature of 100 to 370° C. at a temperature of 100 to 370°C; The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the presence and in the treatment liquid is 1 to 1.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
A step of wet oxidative decomposition at 0 to 370°C, (7) a step of treating the treated liquid obtained in (6) above with activated sludge under normal pressure or pressurization, and (8) a step of treating excess sludge from (7) above. A method for treating wastewater and sludge, comprising the step of returning the wastewater and sludge as described in (5) above. [4] A method for treating wastewater and sludge, comprising (1) crushing kitchen waste into slurry, mixing it with domestic wastewater and/or industrial wastewater, and discharging the mixture into a sewer or a dedicated drain pipe connected to wastewater treatment equipment; (2) a step of separating solids and liquid components in the mixture prior to treatment at a sewage treatment plant or wastewater treatment facility; (3) converting the liquid component separated in (2) above into activated sludge; (4) A step of mixing the solids separated in (2) above and solids generated or recovered in a sewage treatment plant or wastewater treatment facility with sewage; (5) (4) above. The mixture obtained was heated to p in the presence of oxygen.
(6) Wet oxidative decomposition step at a temperature of 100 to 370° C. at a temperature of 100 to 370°C; The theoretical amount of oxygen necessary to decompose ammonia, organic substances, and inorganic substances in the presence and in the treatment liquid is 1 to 1.
pH approximately 1 to 11.5, temperature 10 in the presence of 5 times the amount of oxygen
wet oxidative decomposition at 0 to 370°C; (7) anaerobic methane fermentation treatment of the treated liquid obtained in (6) above; (8) activated sludge treatment of the treated liquid obtained in (7) above. and (9) a step of returning surplus sludge from (7) and/or (8) to (5).