WO2015072740A1

WO2015072740A1 - Method for treating organic waste liquid including sludge and waste water using solvent extraction

Info

Publication number: WO2015072740A1
Application number: PCT/KR2014/010845
Authority: WO
Inventors: 강진구
Original assignee: 김용환
Priority date: 2013-11-15
Filing date: 2014-11-12
Publication date: 2015-05-21
Also published as: KR20150056473A; KR20150056429A; KR20150056471A; KR20150056472A

Abstract

The present invention relates to a method for treating organic waste liquid including sludge and waste water using solvent extraction, comprising the steps of: mixing the organic waste liquid and a solvent so as to extract at least a part of the sludge by the solvent; separating the waste water and the solvent after the extraction; and primarily separating the solvent and the sludge.

Description

Treatment method of organic waste liquid containing sludge and wastewater by solvent extraction

The present invention relates to a method for treating organic waste liquid containing sludge and waste water, and more particularly, to a method for treating organic waste liquid including sludge and waste water using a solvent extraction method.

Under the London Convention, South Korea will ban all dumping of sewage sludge from 2014. Accordingly, the development of technology that can efficiently treat sewage is an urgent reality.

In the existing treatment method, organic sludge, microorganisms and heavy metals existing in sewage are agglomerated / precipitated together with water using a polymer flocculant. According to this treatment method, as shown in FIG. 1, the sludge mass having a specific gravity of about 1.2 is separated / recovered.

The reason for this agglomeration is that water acts as a medium for connecting the particles in a water content of 25% or more.

When the polymer flocculant is used, the water content is 25% or more for two reasons. The first is that organic sludge particles generally have a small particle size of less than 200 m, so that the capillary between them is narrow and the outermost angle cannot be easily removed. The second is that the microorganisms in the sewage are not destroyed. The body water present in the microorganisms accounts for about 40% of the total water after the flocculation treatment.

For this reason, in the conventional method, only 15-20% of water can be dehydrated out of the remaining 60% of the outermost water except for 40% of the body water present in the microorganism through mechanical dehydration.

Therefore, in the existing treatment method, there is a problem that secondary treatment such as heat treatment / dry incineration is required to meet the water content standard for recycling or landfill treatment.

On the other hand, Palm Oil Mill Effluent (POME) is the term used for the wastewater produced when palm oil is produced in a palm oil refining facility. It is causing a big problem.

As such, it is necessary to develop a treatment method for organic waste liquids such as sewage and POME containing organic sludge and waste water.

The present invention is to solve the above problems, an object of the present invention is to provide an organic waste liquid treatment method that is easy to remove the water of the sludge using a solvent extraction method.

The object of the present invention is a method for treating an organic waste liquid containing sludge and waste water by using a solvent extraction method, comprising: extracting at least a portion of the sludge to the organic solvent by mixing the organic waste liquid and the organic solvent; Separating the wastewater and the organic solvent after the extraction; Is achieved by first separating the organic solvent and the sludge.

The sludge includes microorganisms, and the organic solvent includes a microbial destruction component capable of destroying the microorganisms; It may include an interface characteristic change component that can change the characteristics of the sludge interface.

The microbial destruction component includes an alcohol hydrocarbon and may be 3 to 10 wt%.

The interfacial property change component may include an aromatic hydrocarbon and an ether hydrocarbon, the aromatic hydrocarbon may be 19 to 35% by weight, and the ether hydrocarbon may be 5 to 10% by weight.

The organic solvent may further include 29 to 24% by weight of olefinic hydrocarbons and 12 to 29% of paraffinic hydrocarbons.

The sludge includes microorganisms, and the organic solvent includes a microbial destruction component capable of destroying the microorganisms; It may include a viscosity reducing component for reducing the viscosity of the sludge.

The microbial destruction component includes an alcohol-based hydrocarbon, 3 to 10% by weight, and the viscosity reducing component may include 12 to 29% by weight of a paraffinic hydrocarbon.

Before the extraction, the method may further include diluting by adding additional water to the sewage.

Primary separation of the solvent and the sludge may be carried out by a mechanical method.

After the primary separation step of the solvent and the sludge, may further comprise the step of secondary separation of the organic sludge and the solvent under conditions of increasing the vaporization activity.

The secondary separation may be performed at room temperature.

After the primary separation, it may further comprise briquetting or pelletizing the sludge.

The sludge contains a microorganism, the organic solvent includes an alcohol hydrocarbon that can destroy the microorganism, the destruction of the microorganism may be carried out in the extraction step.

The solvent may be reused in the extraction step after recovery in the separation step.

The dilution, extraction and separation steps are carried out in a closed system which is isolated from the outside, wherein the organic waste liquid further comprises oil / grease, and before the extraction, the oil / grease is recovered after mixing the oil recovery solvent and the organic waste liquid. It may further comprise the step.

According to the present invention, there is provided a method for treating an organic waste liquid which is easy to remove water from sludge using a solvent extraction method.

Figure 1 shows the configuration of the aggregated mass obtained in the conventional sludge treatment method,

Figure 2 shows the flow of the sludge treatment method according to a first embodiment of the present invention,

3 illustrates the extraction step in the sludge treatment method according to the first embodiment of the present invention,

4 illustrates the sludge / solvent primary separation step in the sludge treatment method according to the first embodiment of the present invention.

FIG. 5 illustrates the sludge / solvent secondary separation step in the sludge treatment method according to the first embodiment of the present invention.

Figure 6 shows the flow of the sludge treatment method according to a second embodiment of the present invention,

Figure 7 shows the sewage before solvent extraction in the first experimental example,

8 shows the wastewater after the solvent extraction in the first experimental example,

9 shows the sludge powder obtained by the sludge treatment method in the first experimental example,

Figure 10 shows the POME stock solution and diluent in Example 2,

11 shows the treated water in the second experimental example,

12 shows the oil recovered in Example 2,

Figure 13 shows the FT-IR results of the oil recovered in the second experimental example,

14 shows FT-IR results of palm oil on the market in Experimental Example 2.

FIG. 15 shows FT-IR results of a test solvent before use in Example 2,

16 shows the FT-IR results of the experimental solvent recovered after the third experiment in Example 2,

Fig. 17 shows the state of the sludge powder obtained in the second experimental example.

The present invention relates to a method for treating an organic waste solution including sludge and wastewater by using solvent extraction, comprising: extracting at least a portion of the sludge with an organic solvent by mixing sewage and an organic solvent; Separating the wastewater and the organic solvent after extraction; Primary separation of the organic solvent and sludge.

Organic waste liquid in the present invention means a mixture of waste water and sludge. The sludge includes organic sludge, microorganisms and some inorganic substances, and may include only organic sludge in some cases. Organic waste liquid in the present invention is a factory waste water, process waste water, organic waste liquid containing paper slurry, organic waste liquid containing food, organic waste liquid containing livestock manure, organic waste liquid generated after food processing, organic generated in the pharmaceutical process Waste liquid, organic mine wastewater. In addition, the organic waste liquid in the present invention includes a sugar mill effluent (SME) which is a wastewater generated in the process of producing sugar in the sugar cane refinery.

In the present invention, by applying a solvent extraction method used for metal extraction to extract the sludge in the organic waste liquid with an organic solvent, the outermost number of the organic sludge is easily removed in the solvent extraction process. The sludge microorganisms are destroyed by the solvent, so that the crystal water of the microorganism can be easily removed.

In the following description, the sludge includes both organic sludge and microorganisms by way of example. In addition, in the following description, the wastewater and POME are described as organic waste liquids, but the present invention is not limited thereto.

2 to 5, the organic waste liquid treatment method (sludge treatment method) according to the first embodiment of the present invention will be described in detail. The organic waste liquid in the first embodiment is sewage.

2 shows a flow of the sewage treatment method according to the first embodiment.

First dilute the sewage to suit the solvent extraction (S100). Dilution is to adjust the sludge concentration in the sewage in consideration of the reaction ratio between the waste water and the solvent. If the sludge concentration in the sewage is within a range suitable for the solvent extraction process, this step can be omitted. In addition, depending on the sludge concentration in the sewage, process conditions such as solvent usage may be changed in the solvent extraction, in which case the dilution step may be omitted.

In another embodiment, sludge concentrations and / or components in the sewage may be observed and subsequent process conditions may be changed depending on the observed results. Sludge concentrations and / or component observations can be made in real time.

Next, the sludge is extracted by mixing an organic solvent (extraction solvent) and sewage (S200). In this step, solvent extraction is performed in which organic sludge and microorganisms are transferred to an extraction solvent (organic solvent).

The organic solvent is at least two of the microbial destruction components that can destroy microorganisms, the interfacial property change component that changes the characteristics of the sludge interface, the interparticle property change component that changes the characteristics between the sludge particles, and the viscosity reduction component that reduces the viscosity of the sludge It may contain more than branches.

The microbial destruction component functions to destroy microorganisms by leaking internal moisture to the outside of the microbial cell membrane, and may use an alcohol-based hydrocarbon. The alcoholic hydrocarbon may have 2 to 5 carbon atoms, for example, ethanol and / or isopropyl alcohol may be used. Alcoholic hydrocarbons may be used in 3 to 10% by weight.

The interfacial property change component is composed of a first component that increases the water contact angle of the organic sludge interface and a second component that lowers the surface tension of the organic sludge interface. As the first component, an aromatic hydrocarbon may be used, for example, dimethylbenzene and methylbenzene may be used. The first component may be used 19 to 35% by weight. As the second component, an ether hydrocarbon may be used, for example, di-n-propyl ether may be used. The second component may be used 5 to 10% by weight.

The interparticle property change component forms a hydrophobic adsorption agglomerate to widen the capillary radius between organic sludge particles. An olefinic hydrocarbon may be used as the component for changing the particles, for example, 2-methyl 2-butene (di-methyl but-2-ene) and cyclohexane may be used. The interparticle characteristic change component may be used in an amount of 29 to 48 wt%.

The viscosity reducing component performs a function of reducing the viscosity of the organic sludge. As the viscosity reducing component, a paraffinic hydrocarbon having 5 to 8 carbon atoms may be used. For example, pentane, hexane and / or heptane may be used. The viscosity reducing component may be used 12 to 29%.

The specific gravity of the organic solvent may be 0.4 to 0.9, and may be 0.5 to 0.7. Organic solvents may be more volatile than water.

This process will be described in detail with reference to FIG. 3. Organic sludge, microorganisms, wastewater and organic solvents exist before extraction. When mixed, organic sludge particles bind to an organic solvent having a lower specific gravity. Organic sludge particles whose specific gravity is lighter than water through the combination with the organic solvent are separated from the surface water while rapidly moving to the organic solvent layer. In the case of microorganisms, up to 40% of the crystallized water in the microorganisms is easily removed by microbial destruction by organic solvents. Microorganisms combined with organic solvents also migrate to the organic solvent layer.

Extraction may be carried out under turbulent conditions, which may be formed by machinery causing a pressure difference between the inlet and outlet, rheology machines equipped with baffles, mixers or stirrers, and the like. Extraction can be carried out in a batch reaction or in a continuous reaction. In order to improve the extraction rate, it may be performed by co-current multistage extraction or counter-current multistage extraction.

Through this process, organic sludge and microorganisms in sewage are transferred to the organic solvent layer and separated from the waste water.

Next, the waste water phase and the organic solvent phase are separated (S300). This process may use conventional fixing and separation methods. The separated waste water can be used or discharged as industrial / living / agricultural water after appropriate treatment. If necessary, separate concentration tanks can be installed and operated to ensure additional retention time for complete separation of the wastewater from the recovered organic solvent phase. In another embodiment, the separated wastewater may be used for dilution of sewage (S100).

On the other hand, if the sewage contains heavy metals, heavy metals can also be extracted by the organic solvent. In this case, since the heavy metal content of the wastewater is greatly reduced, it is easy to utilize the wastewater. In other embodiments, separate solvents may be used to remove heavy metals in the wastewater or sludge, or additional processes may be added.

Thereafter, the sludge and the organic solvent are first separated (S400). The primary separation can be carried out through any machine capable of solid-liquid separation, such as a vacuum filter, filter press, belt press, screw dehydrator, centrifugal dehydrator. Primary separation may be carried out by a mechanical method, and a single mechanical method may be carried out a plurality of times or a plurality of mechanical methods may be used.

This process will be described in detail with reference to FIG. 4. Organic solvent is combined on the organic sludge and the surface of the microorganism before the first separation. Through primary separation, most organic solvents are recovered from organic sludge and microorganisms.

Next, the organic solvent on the surface of the sludge is secondarily separated (S500).

This process will be described with reference to FIG. 5. Secondary separation of the organic solvent may be carried out at room temperature, and may be compressed air to help recover the remaining organic solvent. Compressed air plays a role in creating a condition that increases the vaporization activity of the organic solvent. Compressed air collides with the organic solvent, and the organic solvent diffuses and vaporizes by the collision. In another embodiment, other means for increasing the vaporization activity of the organic solvent may be used in addition to providing compressed air.

When the secondary separation of the organic solvent is performed at room temperature, there is no separate energy consumption for increasing the temperature, thereby saving energy for organic solvent recovery. In addition, when the organic solvent used is more volatile than water, the energy consumption for obtaining the final sludge is reduced compared to the conventional process.

In another embodiment, the secondary separation may be performed at room temperature to 50, or may use a vacuum.

Secondary separation may be carried out in a batch or continuous process. When carried out in a continuous process it is possible to recover the organic solvent while transporting the sludge to an in-pipe powder transfer device in the form of an air amplifier, a tank containing a rotating body such as a fan, a blower, a cyclone, a jet mill, a conveyor belt or a spiral conveyor.

Secondary separation gives sludge with a water content of less than 10%.

The sludge obtained may be in powder form. Sludge can be manufactured in the form of briquettes or pellets and used as a fuel source, especially with coal where fossil fuels are used, such as thermal power plants and cogeneration plants. The calorific value of the sludge may be 3500 to 5500 kcal / kg.

The organic solvent recovered in the primary separation and the secondary separation can be used again in the extraction process. A process for regenerating all or part of the recovered organic solvent may be added, and a certain amount of organic solvent may be replaced with a new organic solvent.

In another embodiment, the organic solvent replacement time may be automatically informed by observing the extraction efficiency of the organic solvent or the change in the composition of the organic solvent. Observation of extraction efficiency or component change can be made regularly or irregularly, and can be observed in real time. Extraction efficiencies or component changes can be observed by sampling organic solvents or monitored remotely through instruments.

The treatment of sewage described above can be carried out in a closed system in which the outside and the inside are separated. In this case, the occurrence of other additional reactions is inherently blocked and the risk of secondary environmental pollution is reduced.

Referring to Figure 6 will be described in the organic waste liquid treatment method according to a second embodiment of the present invention. In the second embodiment, the organic waste liquid is POME.

Palm Oil Mill Effluent (POME) is the term used for the wastewater produced when palm oil is produced in a palm oil refinery. It is not easy to treat wastewater, which is a major environmental problem in six Southeast Asian countries that are currently producing palm oil. Is causing.

In Malaysia, about 172 million tons are generated annually in 430 Palm Oil Mills, and the amount is increasing every year. POME has a very high BOD, COD concentration, as well as a large amount of Total Solids, Suspended Solids, Volatile solids, and Oil & Grease.

Table 1 shows the general characteristics of POME.

<Table 1> General Properties of POME (mg / L, pH Excluded)

Table 1

Parameter	Average	range	Regulatory Levels (Malaysia)
pH	4.2	3.4-5.2	5-9
Biological oxygen demand (BOD)	25,000	10,250-43,750	100
Chemical oxygen demand (COD)	51,000	15,000-100,000	-
Total solids	40,000	11,500-79,000	-
Suspended Solids	18,000	5,000-54,000	400
Volatile solids	34,000	9,000-72,000	N / A
Oil and grease	6,000	130-18,000	50
Ammoniacal Nitrogen	35	4-90	100

Currently applied POME treatment technologies include 1) Ponding system, 2) Conventional physico-chemical treatment, and 3) Aerobic and Anaerobic digestion. have. However, most of the slow treatment times (reservoir treatment: 45-60 days, aerobic & anaerobic treatment: 4-10 days), large treatment sites, difficulties in managing volatile gas capture and capture systems such as methane and high water content of sediments (more than 80%) Due to problems such as), POME is not properly handled.

A part different from the first embodiment of the second embodiment is the oil / grease recovery step S150. In the oil / grease recovery step (S150), the oil and grease residues contained in the POME are separated / recovered, and an extraction method using an oil recovery solvent may be used.

The oil recovery solvent may consist of aromatic hydrocarbons and paraffinic hydrocarbons. The aromatic hydrocarbon may use dimethylbenzene and / or methylbenzene, and the paraffinic hydrocarbon may use pentane, heptane and / or octane. The aromatic hydrocarbon may be used 74 to 95% by weight, more specifically 22 to 81% by weight of dimethylbenzene and 14 to 53% by weight of methylbenzene may be used. The paraffinic hydrocarbon may use 5 to 26% by weight of C5 to C12 hydrocarbon. More specifically, 2 to 13 wt% of pentane, 2 to 8 wt% of heptane, and 1 to 5 wt% of octane may be used. As the paraffinic hydrocarbon, hexane, nonane, decane, undecane and / or dodecane can be used.

Oil / grease recovery recovers oil recovery solvents containing oil and grease. The recovered oil recovery solvent can be used as an energy source of oil components by itself, and can be separated from oil and grease through a special separation device such as a heating / aggregation recovery device or a membrane separator.

According to the present invention as described above, even microorganisms are destroyed and odor can be removed, and the sludge is recycled and waste treatment costs are not incurred. Dewatering of the sludge is easy, which greatly reduces the energy cost for dewatering. The treatment of waste water can also take place in a closed system, thus suppressing the occurrence of unwanted reactions and reducing the risk of secondary environmental pollution. In addition, since it does not affect the wastewater treatment efficiency of the existing sewage treatment plant, it is easy to install as an auxiliary device in an existing facility, and it is also possible to replace an existing dewatering system. In addition, it is easy to equip large-capacity facilities through device-intensive processes.

Dilution (S100) and other steps are similar to the first embodiment and can be modified by those skilled in the art as appropriate.

The present invention will be described in more detail with reference to the following experimental examples.

Experimental Example 1 Sewage Treatment

The sewage used for the experiment was taken from the U city Y sewage treatment plant, showing a turbid state as shown in FIG. MLSS (mixed liquor suspended solids) was 5027 mg / L.

Sewage and organic solvent were mixed at a volume ratio of 1: 0.0005 at room temperature, and the solvent was extracted under turbulent conditions for 5 minutes.

The composition of the organic solvent used is as follows.

TABLE 2

Ingredient Name	content (%)
Dimethylbenzenes	8
Methylbenzene	19
Ethanol	4
Isopropyl alcohol	3
Di-n-propyl ether	7
2-methyl but-2-ene	26
Cyclohexane	13
Heptane	10
Hexane	6
Pentane	4

8 shows the wastewater from which the organic solvent phase is separated after standing, and shows that the sludge has been sufficiently removed as compared with FIG. 7.

9 collects organic sludge powder dried through primary and secondary separations.

Table 3 below is the component and calorific value data of the organic sludge recovered. The high calorific value was 3,876 kcal / kg, which is sufficient for thermal power plants.

TABLE 3

Test Items	unit	Result ¹⁾	Test Methods
Fixed carbon	%	9.2	ASTM D 5142-04 (Compliant)
Ash	%	6.2	ASTM D 5142-04 (Compliant)
Volatile Powder (VM)	%	78.9	ASTM D 5142-04 (Compliant)
moisture	%	3.7	ASTM D 5142-04 (Compliant)
Sulfur powder	%	0.37	KS E ISO 334: 2003
High calorific value	kcal / kg	3876	KS E 3707: 2001 (applied mutatis mutandis)

1) The remaining 1.63% is other components such as nitrogen and phosphorus.

Experimental Example 2 POME Treatment

The experiment was performed on POME with an MLSS concentration of 57,400 (mg / L). After 20-fold dilution, POME and an oil recovery solvent were mixed at turbulent conditions for 5 minutes at a volume ratio of 1: 0.0005, and oil and grease were recovered. Thereafter, the POME and the organic solvent were mixed at turbulent conditions for 5 minutes at a volume ratio of 1: 0.0005, and then the solvent phase and the wastewater phase were separated.

The composition of the oil recovery solvent is shown in Table 4, and the composition of the organic solvent is the same as in Experiment 1.

Table 4

ingredient	content%
Dimethylbenzenes	55
Methylbenzene	35
Pentane	5
Heptane	3
Octane	2

Figure 10 shows the POME stock solution and diluent, and Figure 11 shows the treated water.

The experimental results are as follows.

<Table 5> Water quality analysis results (mg / L) of POME stock solution, diluent solution and treated water

Table 5

Analysis item	Stock solution	diluent	Treated water	Removal rate (%) ¹⁾
pH ²⁾	3.7	4.2	4.3	-
BOD ²⁾	27600	1070	514	52.0
COD ²⁾	25000	1000	605	39.5
Total Solid (TS) ³⁾	50900	2280	-	-
Volatile Solid (VS) ³⁾	41100	1790	-	-
Suspended Solid (SS) ²⁾	9200	520	48.4	90.7
Oil and Grease (O & G) 2)	1800	80	7.9	90.1
Ammoniacal Nitrogen (NH ₄ ⁺ ) ²⁾	85.4	4.95	3.91	21.0

Note 1) The removal rate is calculated from the concentration ratio of the dilution standard treatment water for each item.

2) Test according to water pollution process test standard: 2012

3) Test according to APHA Standard Methods: 2012

Table 5 shows the results of water quality analysis by sampling the treated water obtained after the solid sludge (SS) separation experiment in the POME diluent. As can be seen in Table 5, SS and O & G, which are to be removed in this experiment, can satisfy both Malaysian regulations.

For each item, SS showed 90.7% removal efficiency compared to diluent and 90.1% for O & G.

In addition, it was confirmed that an additional effect of removing 52% of the dilution water in the case of BOD and 39.5% in the case of COD, although not the treatment target of the present technology.

FT-IR analysis was performed to confirm that the oil components of the recovered oil were the same as the palm oil. Figure 12 shows the recovered oil, Figure 13 shows the FT-IR results of the recovered oil, Figure 14 shows the FT-IR results of commercially available palm oil.

As can be seen from the analysis results, it can be seen that the FT-IR results of FIGS. 13 and 14 show nearly identical transmittance peaks at the same wavenumber. Therefore, the recovered oil was confirmed to be palm oil through this experiment.

FT-IR analysis of the organic solvent (fresh) and the organic solvent (used) recovered after the third experiment before using the palm oil was performed in the same manner as in the analysis method of palm oil to confirm the appearance of the peak. FIG. 15 shows FT-IR results of the organic solvent before use, and FIG. 16 shows FT-IR results of the organic solvent recovered after the third experiment.

As can be seen in Figures 15 and 16 it can be seen that almost the same transmittance peak appears at the same wavenumber. Therefore, the recovered organic solvent was confirmed that no deformation occurs in the extraction experiment process, and it was confirmed experimentally that the same extraction efficiency is obtained when actually reused using this organic solvent.

In this experiment, high calorific value of the recovered powder was analyzed to confirm the possibility of solid fuelization of the powder recovered from POME. Figure 17 shows the state of the sludge powder obtained in the second experimental example of the present invention.

TABLE 6 High calorific value of powder recovered from POME

Table 6

Test Items	unit	Result	Test Items
moisture	%	4.3	ASTM D 5142-04 (Compliant)
High calorific value	J / g	17800	KS E 3707: 2001 (applied mutatis mutandis)

As can be seen in Table 6, the recovered powder had a high calorific value of 17800 J / g. This translates into a calorific value of about 4252 kcal / kg, which is sufficient for thermal power plants.

As can be seen from the results in this experimental example, the POME can be effectively treated by the present invention.

Although the present invention has been described with reference to one embodiment shown in the accompanying drawings, this is merely exemplary, and it will be understood by those skilled in the art that various modifications and equivalent other embodiments are possible. Could be. Accordingly, the true scope of protection of the invention should be defined only by the appended claims.

The present invention can be used for the treatment of organic waste liquid.

Claims

In the method of treating the organic waste liquid containing the sludge and waste water using a solvent extraction method,

Mixing at least a portion of the sludge with the organic solvent by mixing the organic waste liquid and the organic solvent;

Separating the wastewater and the organic solvent after the extraction;

Organic waste liquid treatment method comprising the step of primary separation of the organic solvent and the sludge.
The method of claim 1,

The sludge contains microorganisms,

The organic solvent,

Microbial destruction components capable of destroying the microorganisms;

An organic waste liquid treatment method comprising an interface characteristic change component capable of changing the characteristics of the sludge interface.
The method of claim 2,

The microorganism destruction component comprises an alcohol-based hydrocarbon, organic waste solution treatment method characterized in that 3 to 10% by weight.
The method of claim 3,

The interfacial property change component includes an aromatic hydrocarbon and an ether hydrocarbon, wherein the aromatic hydrocarbon is 19 to 35% by weight and the ether hydrocarbon is 5 to 10% by weight.
The method of claim 3,

The organic solvent further comprises 29 to 24% by weight of an olefinic hydrocarbon and 12 to 29% of a paraffinic hydrocarbon.
The method of claim 1,

The sludge contains microorganisms,

The organic solvent,

Microbial destruction components capable of destroying the microorganisms;

An organic waste liquid processing method comprising a viscosity reducing component for reducing the viscosity of sludge.
The method of claim 6,

The microbial destruction component comprises an alcohol hydrocarbon and 3 to 10% by weight,

The viscosity reducing component is an organic waste liquid treatment method comprising a paraffinic hydrocarbon, 12 to 29% by weight.
The method of claim 1,

Before the extraction,

And further diluting by adding additional water to the sewage.
The method of claim 1,

Primary separation of the solvent and the sludge is characterized in that the organic waste liquid treatment method performed by a mechanical method.
The method of claim 9,

After the first separation step of the solvent and the sludge,

The organic waste liquid treatment method further comprises the step of separating the organic sludge and the solvent in the conditions of increasing the vaporization activity.
The method of claim 1,

The secondary separation is organic waste liquid treatment method characterized in that carried out at room temperature.
The method of claim 1,

After the first separation,

Briquetting or pelletizing the sludge organic waste liquid treatment method characterized in that it further comprises.
The method of claim 1,

The sludge contains microorganisms,

The organic solvent includes an alcohol hydrocarbon capable of destroying the microorganism,

Destruction of the microorganism,

Organic waste liquid treatment method characterized in that carried out in the extraction step.
The method of claim 1,

The solvent,

Organic waste solution treatment method characterized in that for reuse in the extraction step after the recovery in the separation step.
The method of claim 1,

The dilution, extraction and separation steps are carried out in a closed system isolated from the outside,

The organic waste liquid further comprises an oil / grease,

Before the extraction, further comprising the step of recovering the oil / grease after mixing the oil recovery solvent and the organic waste liquid.