JP2015144990A - Waste liquid treatment apparatus - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a waste liquid treatment apparatus capable of effectively using the heat energy generated by oxidative decomposition of organic substance, contributing to reduction of running costs.SOLUTION: The inside of a reaction vessel 11 is divided by a cylindrical partition member 12 into a first compartment 11A located outside the partition member 12 and a second compartment 11B located inside the partition member 12. An upper surface side of the first compartment 11A is connected with an introduction pipe 9 for introducing a fluid mixture of a waste liquid and an oxidizer, and an upper surface side of the second compartment 11B is connected with a discharge pipe 16 for discharging a processed fluid. The fluid mixture of the waste liquid and the oxidizer flows downward in the first compartment 11A, then changes the flow direction upward in a folding space 11C, and flows upward in the second compartment 11B. A catalyst for accelerating the oxidation is installed in the second compartment 11B, so that the heat generated by the oxidation of organic substances moves to the first compartment 11A, helping the first compartment 11A attain higher temperature.

Description

  The present invention relates to a waste liquid treatment apparatus in which an object to be treated such as waste water is mixed with an oxidant such as air, and an organic substance is decomposed by a hydrothermal oxidation reaction under a high temperature and high pressure condition.

Conventionally, incineration and biological treatment methods are known as methods for detoxifying waste liquids and wastes containing organic substances.
However, in the case of incineration, enormous energy and new chemicals are required for dehydration and solid content aggregation as pretreatment.
Moreover, since the combustion temperature of an incinerator is reduced at the time of incineration, it is inevitable that dioxins are generated.
In the case of biological treatment, the treatment time is extremely long, and there is a problem that activated sludge generated after treatment becomes a new waste.

As one of the technologies to solve these problems, the water in the waste liquid is changed to a supercritical state, a superheated steam state, or a subcritical state in a high-temperature and high-pressure environment, and the organic matter in the waste liquid is decomposed in a short time. Development of waste liquid treatment equipment has started.
In the subcritical liquid, organic substances are hydrolyzed. Further, in a supercritical state or superheated steam state liquid, organic substances are oxidatively decomposed by mixing with an oxidizing agent.
For this reason, even a high-concentration organic solvent waste liquid or a plastic solid-containing waste liquid, which was impossible with biological treatment, can be easily treated.
Even a waste liquid containing a large amount of organic organic solids can be decomposed into water, nitrogen gas, and carbon dioxide by almost completely oxidizing and decomposing the organic matter.

In an apparatus for processing in a high-temperature and high-pressure environment, the liquid to be treated is generally introduced from the upper part of the vertical reactor and discharged from the upper part using the folding phenomenon at the lower part.
However, in the configuration in which it is folded in one reactor, there is a problem that undecomposed organic matter in the liquid to be treated is mixed with the processing liquid and discharged.
In order to cope with this problem, a configuration has been proposed in which a partition member is installed in the reactor and the inflow port of the liquid to be processed and the outflow port of the process liquid are completely partitioned (Patent Document 1).

By the way, it is known that the organic matter contained in the object to be treated generates heat when it is oxidatively decomposed in the reactor and can contribute to maintaining the reactor at a high temperature. The heat generated when the organic matter is oxidatively decomposed is a by-product, and if this heat is used as a means for suppressing the temperature drop on the introduction side of the object to be processed, the reactor is heated with a heater or the like. Heat energy can be reduced, leading to a reduction in running costs.
Considering the configuration partitioned by the partition members disclosed in Patent Document 1 and the like from the viewpoint of heat transfer for utilizing the heat generated when the organic matter is oxidatively decomposed, the partition where the oxidation process proceeds becomes high temperature Is in contact with the inner surface of the reactor having a large heat transfer area, and heat transfer in the reactor is generally dissipated toward the outside of the reactor.
For this reason, it has not reached the level which raises the temperature fall in the introduction side of a to-be-processed object, and brings about the reduction | decrease in thermal energy.

  The present invention has been made in view of such a situation, and can provide a waste liquid treatment apparatus that can efficiently use thermal energy generated by oxidative decomposition of organic matter and contribute to a reduction in running cost. Main purpose.

  In order to achieve the above-described object, the waste liquid treatment apparatus of the present invention is a mixture of an object to be treated containing an organic substance and an oxidizing agent, or is introduced separately, and the water is supercritical water, superheated steam, or subcritical water. A reactor for decomposing the organic matter by an oxidation reaction, and extending from one end side to the other end side of the reactor, and the inside of the reactor includes the object to be treated and the oxidizing agent. And a partition member that divides the first compartment into which the treated fluid is discharged and a second compartment having a discharge port that discharges the processed fluid, and the partition member has the mixed fluid of the first compartment It is arranged so as to flow from one end side toward the other end side, bend back at the other end side, and flow in the second compartment in the direction opposite to the first compartment, and the heat of the second compartment is Heat transfer is controlled so that it moves through the partition member. It has a configuration that.

  According to the present invention, heat energy generated by oxidative decomposition of an organic substance can be efficiently used, which can contribute to a reduction in running cost.

1 is a schematic configuration diagram of a waste liquid treatment apparatus according to a first embodiment of the present invention. It is a longitudinal cross-sectional view of the principal part of a reactor. It is a longitudinal cross-sectional view which shows the internal structure of the reactor of the waste liquid processing apparatus which concerns on 2nd Embodiment. It is a longitudinal cross-sectional view which shows the internal structure of the reactor of the waste liquid processing apparatus which concerns on 3rd Embodiment. It is a figure which shows the internal structure of the reactor which concerns on 4th Embodiment, (a) is a longitudinal cross-sectional view of the principal part of a reactor, (b) is a cross-sectional view in the XX line of (a), c) is a cross-sectional view taken along line YY of (a). It is a longitudinal cross-sectional view which shows the apparatus structure of an Example.

Embodiments of the present invention will be described below with reference to the drawings.
First, a first embodiment will be described based on FIGS. 1 and 2.
FIG. 1 is a block diagram schematically showing the overall configuration of the waste liquid treatment apparatus according to this embodiment.
A waste liquid treatment apparatus (waste liquid treatment system) 50 includes a waste liquid tank 1, a stirrer 2, a waste liquid supply pump 3, a waste liquid inlet valve 4, an air introduction pipe 5, a compressor 6, an oxidant inlet valve 7, a reactor 10, a cooling unit 20, A heat exchange pump 22, a filter 23, an outlet pressure gauge 24, a back pressure valve 25, a gas-liquid separator 26, a control unit (not shown), and the like are provided.
The reactor 10 includes a cylindrical and vertical reaction vessel 11, a heater 15 for heating the reaction vessel 11, temperature sensors 17 a and 17 b for detecting the temperature in the reaction vessel 11, and the like.

“Inside the reactor” means substantially inside the reaction vessel 11. The interior of the reaction vessel 11 is divided into a first compartment 11A and a second compartment 11B by a cylindrical (tubular) partition member 12.
The partition member 12 is formed of a member having heat conductivity.

The waste liquid tank 1 is a container for storing a waste liquid containing an organic substance having a relatively large molecular weight, which becomes an object to be processed.
The waste liquid is one of an organic solvent, an aqueous solution containing an organic solvent, a slurry containing an organic solid, a solid waste containing an organic substance, or a combination thereof.
The stirrer 2 is for uniformizing the dispersion of the organic solids in the waste liquid by stirring the waste liquid.

The waste liquid in the waste liquid tank 1 is fed by the waste liquid supply pump 3 and supplied to the reaction vessel 11 through the waste liquid inlet valve 4.
The waste liquid supply pump 3 is controlled by a control unit (not shown) so that the liquid flow rate is constant.
When the waste liquid needs to be heated, a preheater may be installed between the waste liquid inlet valve 4 and the reactor 10.

The compressor 6 sucks air in the atmosphere as an oxidant and sends it toward the reaction vessel 11 while compressing it to a pressure comparable to the inflow pressure of the workpiece.
The amount of the oxidant fed by driving the compressor 6 is determined based on the stoichiometric amount of oxygen necessary to completely oxidize the organic matter in the waste liquid.
The driving of the compressor 6 is controlled by the control unit, and the inside of the reaction vessel 11 is pressurized to a predetermined pressure and maintained.

As the oxidant, any one of air, hydrogen peroxide solution, oxygen gas, ozone gas, or a mixture of two or more of them can be used.
The oxidant inlet valve 7 adjusts the flow rate of the oxidant supplied to the reaction vessel 11.
When the oxidant needs to be heated, a preheater may be installed between the oxidant inlet valve 7 and the reactor 10.

As described above, the object to be processed supplied from the waste liquid supply pump 3 and the oxidizing agent supplied from the compressor 6 are introduced into the reaction vessel 11.
The object to be processed and the oxidizing agent are mixed in the introduction pipe 9 and then introduced into the reaction vessel 11.
However, the present invention is not limited to this, and a plurality of introduction pipes may be provided so that the object to be processed and the oxidizing agent are separately introduced into the reaction vessel 11 and mixed inside the reaction vessel 11. Hereinafter, the mixed fluid is referred to as a mixed fluid M.
In the reaction vessel 11, the object to be treated is oxidatively decomposed by an oxidation reaction within a pressure range of 0.5 to 30 MPa (desirably 5 to 30 MPa).
The pressure in the reaction vessel 11 is detected by an outlet pressure gauge 24 and adjusted by a back pressure valve 25 described later.

In the reaction vessel 11, the object to be treated is oxidatively decomposed at a temperature in the range of 100 to 700 ° C. (preferably 200 to 550 ° C.).
The temperature in the reaction vessel 11 is detected by the temperature sensors 17a and 17b, and the temperature is adjusted by the heater 15 controlled by the control unit.
The temperature sensor 17a detects the temperature inside the partition member 12 (second section), and the temperature sensor 17b detects the temperature outside the partition member 12 (first section).
So as to oxidatively decompose the object to be treated under the condition that the water is in the supercritical state, the temperature is higher than the critical temperature of water (374.2 ° C.) and lower than 700 ° C., the pressure is higher than the critical pressure of water (22.1 MPa) It may be.
When the object to be treated comes into contact with the oxidant in the supercritical water, the oxidative decomposition of the organic substance in the object to be treated can be efficiently performed.

You may make it oxidatively decompose a to-be-processed object on the conditions whose temperature is 200 degreeC or more and a pressure is less than 22.1 MPa, ie, water becomes superheated steam or subcritical water.
In this case, since the rate of oxidative decomposition of the organic substance in the object to be processed is reduced as compared with the condition for achieving the supercritical state, a catalyst that promotes oxidative decomposition may be installed in the reaction vessel 11 as necessary. .
In the reaction vessel 11, heat is generated due to oxidative decomposition of organic substances in the object to be processed. When the concentration of the organic substance in the object to be processed is sufficiently high, the temperature in the reaction vessel can be maintained by the heat generated during the oxidative decomposition without using the heater 15.
Although specifically described later in the first compartment and the second compartment in the reaction vessel 11, the organic matter in the object to be treated is obtained by bringing the mixed fluid containing the object to be treated into a high temperature and high pressure state. Oxidative decomposition.

A heat exchange medium is sent to the cooling unit 20 by a heat exchange pump 22.
The treated fluid is heat exchanged with the heat exchange medium and cooled. The treated fluid that has passed through the cooling unit 20 is depressurized by the back pressure valve 25 after removing the fine particles through the filter 23.

The treated fluid is separated into treated water and gas by the gas-liquid separator 26.
The treated water separated by the gas-liquid separator 26 is obtained by almost completely oxidizing and decomposing organic matter, and only contains minute inorganic solids and inorganic salts that cannot be decomposed and have passed through the filter 23. It is.
If the inorganic solid content and salt are removed from the treated water, it can be reused as industrial water.
The gas separated by the gas-liquid separator 26 is mainly composed of carbon dioxide, nitrogen, and oxygen gas, and can be directly released into the atmosphere.

Next, based on FIG. 2, the structure in the reaction container 11 is demonstrated in detail.
FIG. 2 is a longitudinal sectional view of the reaction vessel 11. A heater 15 is installed so as to surround the outer surface of the reaction vessel 11.
As described above, the inside of the cylindrical reaction vessel 11 is divided into the second partition 11B and the outside by the small-diameter cylindrical partition member 12 fixed to the upper surface 11a as one end side. It is divided as the first section 11A.
In this embodiment, the partition member 12 is disposed so as to be concentric with the reaction vessel 11.

  An inlet pipe 9 for introducing the mixed fluid M is connected to the upper surface side of the first section 11A, and a discharge pipe (discharge port) for discharging the processed fluid is connected to the upper surface side of the second section 11B. ) 16 is connected. The lower end of the partition member 12 is not in contact with the bottom surface 11b as the other end side of the reaction vessel 11, and a fluid return space 11C is provided on the bottom surface side.

The mixed fluid M introduced from the introduction pipe 9 flows downward in the first section 11A.
The mixed fluid M that has come out of the first section 11A changes its flow direction from downward to upward in the folded space 11C and flows into the second section 11B.
In the second section 11B, a plurality of fins 18 are fixed over substantially the entire vertical direction. The fin 18 is formed of a heat conductive member.
A catalyst 19 is disposed on the surface of the fin 18 and the inner peripheral surface of the partition member 12.
The mixed fluid M is brought into contact with the catalyst 19 in the process of flowing through the second section 11B, whereby oxidation is promoted, and flows toward the discharge pipe 16 while contacting the catalyst 19 upward from below.

  The catalyst contains one or more of Ru, Pd, Rh, Pt, Au, Ir, Os, Fe, Cu, Zn, Ni, Co, Ce, Ti, and Mn as active species.

As described above, the mixed fluid M containing organic matter comes into contact with the catalyst when flowing through the second compartment 11B.
By contacting the organic substance and the catalyst, the organic substance contained in the mixed fluid is oxidatively decomposed by the catalytic action.
At this time, heat due to oxidation is generated in the second compartment 11B due to oxidation of the organic matter.

Heat due to oxidation in the second compartment 11B can be transferred to the first compartment 11A having a temperature lower than that of the second compartment 11B via the partition members 12 and the fins 18 having heat conductivity.
The heat transfer from the second section 11B contributes to a higher temperature for maintaining a good oxidation treatment in the first section 11A.
In other words, it is possible to reduce the amount of heating energy supplied to the reaction vessel 11 by the heater 15 for maintaining the temperature in the reaction vessel 11 that is lowered by the sequentially introduced mixed fluid M at a predetermined temperature.
Reduction in the amount of heating energy supplied contributes to a reduction in running cost of the waste liquid treatment apparatus.

The partition member 12 is made of a Ni-based alloy having heat conductivity and corrosion resistance, but is not limited to this, and Ti, stainless steel, or the like may be used.
As a material of the partition member 12, it is possible to employ Fe, Ni, Ti, Ta, Cu, Ag, Au, Pt, Ir, Rh, Pd, Al, Cr, or an alloy in which two or more of these are combined. it can.
Since there is almost no fluid pressure difference between the second compartment 11B and the first compartment 11A in the reaction vessel 11, the partition member 12 needs almost no strength to hold the fluid.
Therefore, the thickness of the partition member 12 can be reduced. The thinning of the partition member 12 makes it easier to transfer heat from the second section 11B to the first section 11A.

The heat in the second compartment 11B can be moved directly to the first compartment 11A via the partition member 12. That is, since heat transfer is performed in one reaction vessel, there is almost no loss of heat exchange.
Moreover, in this embodiment, since it has the structure which arrange | positions the 1st division 11A with low temperature on the outer side of the partition member 12, the thermal radiation to the exterior of the reaction container 11 can be suppressed low, and the heat exchange efficiency of a reactor Will be expensive.
Further, the heat transfer area in the second section 11B is widened by the fins 18 in the second section 11B.
Thereby, the amount of heat transferred from the second section 11B to the first section 11A through the partition member 12 can be increased. That is, the responsiveness of heat exchange can be improved.

In the present embodiment, the fluid flow in the first compartment 11A and the fluid flow in the second compartment 11B are opposed to each other and are in opposite directions.
With the configuration as described above, the heat generated in the second compartment 11B is efficiently transferred to the first compartment 11A via the partition member 12, thereby improving the thermal efficiency in the reactor.
As described above, in the present embodiment, the heat transfer is controlled so that the heat of the second compartment 11B having a high temperature moves to the first compartment 11A having a low temperature via the partition member 12. ing.

The “configuration for controlling heat transfer” in the present embodiment is a configuration itself in which the inside of the partition member 12 is the second section.
In this case, heat transfer from the second section 11B to the first section 11A naturally occurs without providing a member having heat conductivity such as the fin 18.
“Controlling the heat transfer” means that the temperature of the first section 11A is raised to reduce the amount of heat energy supplied by the heater 15 and the running cost can be reduced to the first section 11A. Means directing heat transfer.

A second embodiment will be described with reference to FIG.
Note that the same parts as those in the above embodiment are denoted by the same reference numerals, and unless otherwise specified, description of the configuration and functions already described is omitted, and only the main part will be described (the same applies to other embodiments below).
As shown in FIG. 3, in this embodiment, the inside of the partition member 12 is the first compartment 11A, and the outside is the second compartment 11B.
The waste liquid introduction pipe 9a and the oxidant introduction pipe 9b are separately connected to the upper surface side of the first section 11A, and the upper side surface of the second section 11B is a discharge for discharging the processed fluid. The tube 16 is connected substantially horizontally.

The waste liquid W and the oxidizing agent H are mixed in the first compartment 11A to become a mixed fluid M.
The mixed fluid M in the first section 11A flows downward, changes its direction upward in the folded space 11C, and enters the second section 11B.
A plurality of fins 32 having heat conductivity are fixed to the outer peripheral surface of the partition member 12 at intervals in the vertical direction.
A catalyst 27 is disposed on the outer peripheral surface of the partition member 12, the surface of the fin 32, and the inner peripheral surface of the reaction vessel 11.
The mixed fluid containing the organic substance comes into contact with the catalyst 27 when flowing through the second section 11B, and the organic substance contained in the mixed fluid is completely oxidized and decomposed by the catalytic action.
Oxidation of the organic matter generates heat due to oxidation in the first compartment 11A and the second compartment 11B. In the present embodiment, since the oxidative decomposition is promoted by catalytic action in the second compartment 11B, the temperature of the second compartment 11B is higher than that of the first compartment 11A.

The area (heat transfer area) of the inner peripheral surface of the reaction vessel 11 is larger than the area (heat transfer area) of the outer peripheral surface of the partition member 12.
Further, the second section 11B is arranged outside where the amount of heat released from the reaction vessel 11 increases. For this reason, the heat generated in the second section 11B roughly moves to the outside having a large heat transfer area, and does not contribute much to the temperature increase in the first section 11A.
In the present embodiment, in order to solve this problem, as described above, a plurality of fins 32 are provided on the outer peripheral surface of the partition member 12 to increase the heat transfer area on the first section 11A side.
Thereby, the heat which generate | occur | produces in the 2nd division 11B is efficiently moved to 11 A of 1st divisions via the partition member 12, and the thermal efficiency in a reactor is improved.

  The “configuration for controlling heat transfer” in the present embodiment is based on the original heat transfer area of the partition member 12 (heat transfer area on the first partition side) by adding fins 32 that are members having heat transfer properties. Is also widened.

A third embodiment will be described with reference to FIG.
The arrangement relationship between the first section 11A and the second section 11B is the same as in the second embodiment.
In the present embodiment, in order to efficiently move the heat generated in the second compartment 11B to the first compartment 11A via the partition member 12, the shape of the partition member 12 is changed to obtain the original heat transfer area. It is also wide.
Specifically, the side surface of the partition member 12 is bent to form a bellows shape as a whole.

Thereby, the heat transfer area on the first section 11A side is increased, and the heat generated in the second section 11B can be efficiently moved to the first section 11A via the partition member 12.
Instead of the bent shape, the heat transfer area may be widened by providing irregularities on the surface of the partition member 12. In the present embodiment, the catalyst 27 is disposed on the inner and outer surfaces of the partition member 12 and the inner surface of the reaction vessel 11.

A fourth embodiment will be described with reference to FIG.
The arrangement relationship between the first section 11A and the second section 11B is the same as in the second embodiment.
As shown in FIG. 5A, the second compartment 11B is filled with a granular catalyst 29 that promotes oxidative decomposition of organic matter.
As shown in FIG. 5B, heat transfer plates 34 extending in the vertical direction are radially arranged on the outer peripheral surface of the partition member 12 (omitted in FIG. 5A).

The “configuration for controlling heat transfer” in the present embodiment is made wider than the original heat transfer area of the partition member 12 by adding a plate 34 that is a member having heat transfer properties.
Thereby, the heat transfer area on the first section 11A side is increased, and the heat generated in the second section 11B can be efficiently moved to the first section 11A via the partition member 12.

In the present embodiment, the bottom surface of the reaction vessel 11 is extended to provide a solid matter storage section 11D for depositing and depositing inorganic solid matter that precipitates during processing. That is, a means for separating and removing inorganic solids is provided.
When the waste liquid containing a lot of inorganic solids is treated, there is a problem that the inorganic solids are deposited in the apparatus during the treatment, the piping and the reactor are blocked, and the treatment efficiency is lowered.
In the oxidation treatment under high temperature and high pressure, the waste liquid is introduced into a high temperature and high pressure reactor through a pipe.
When the temperature of the waste liquid is increased under high pressure conditions, and the water becomes supercritical or superheated steam, the density of the water is greatly reduced. A solid inorganic solid is deposited.
Inorganic salts that have been dissolved in the waste liquid may be deposited in the pipe.

Since the ability to transport water also decreases under conditions of high temperature and pressure, solids such as these inorganic solids and inorganic salts often precipitate and accumulate in the apparatus piping and close the piping.
If the inorganic solids dispersed in the waste liquid before being introduced into the reactor are removed by general methods such as precipitation and agglomeration, the amount of inorganic solids deposited in the reactor will be reduced and the equipment will be clogged. Can be prevented.
However, in this case, organic matter is also removed in addition to the inorganic solid matter.
The organic matter is oxidized and decomposed with supercritical water or superheated steam at high temperature and high pressure, and is reduced in molecular weight and dissolved in the fluid. Therefore, there is almost no influence on the clogging of the reactor.
When the organic matter is removed, the heat energy due to the decomposition of the organic matter cannot be used, and the running cost becomes high.

  In this embodiment, it aims at coexistence with the improvement of the thermal efficiency in a reactor, and separating and removing an inorganic solid substance efficiently.

In the upper part of the first section 11A, the object to be processed and the oxidizing agent are mixed.
The mixed fluid M of the object to be processed and the oxidizing agent is heated by heat or the like moving from the second section 11B, so that water changes from a liquid state to a supercritical state or a superheated steam state.
At this time, the inorganic solids dispersed in the water are separated from the water and deposited. Then, it sinks downward in the vertical direction due to gravity.
On the other hand, the organic solid substance dispersed in water is dissolved in supercritical water or superheated steam under high temperature and high pressure by reducing the molecular weight in the first compartment 11A.
Specifically, a part of the organic matter dispersed in water is oxidatively decomposed or reduced in molecular weight by supercritical water, superheated steam or a catalyst under high temperature and high pressure.
The organic matter is dissolved in supercritical water or superheated steam under high temperature and pressure by being oxidatively decomposed or reduced in molecular weight and mixed with the mixed fluid M.

The mixed fluid M and the inorganic solid S in the first section 11A proceed to the folding space 11C. However, since the inorganic solid has a higher density than the mixed fluid, as shown by the dotted arrow in the figure, the gravity drop To enter the solid storage compartment 11D and deposit.
In this embodiment, gravity is used for the separation of the inorganic solid S and the mixed fluid M in this way, and in order to enable this gravity separation, the reactor 10 is placed with one end on the upper side and the other end with the lower side. It is a vertical type on the side.
When separation of the inorganic solid S and the mixed fluid M is performed by another means, the flow direction of the fluid is not limited to this embodiment.

The mixed fluid M flowing into the second compartment 11B is in a state in which the inorganic solid matter is completely removed.
Since the inorganic solid matter is deposited on the bottom of the reaction vessel 11, the reaction vessel 11 is not blocked by the inorganic solid matter.

[Example 1]
Examples for confirming the effects of the present invention will be described below.
As shown in FIG. 6, the experiment was performed using the configuration shown in FIG. The temperature sensor 35a is arranged so as to measure the inlet temperature of the first section 11A, and the temperature sensor 35b is arranged so as to measure the outlet temperature of the first section 11A.
The temperature sensor 35c is disposed at the center of the second section 11B in the vertical direction so that the average temperature of the second section 11B can be measured.

Table 1 shows the operating conditions and the temperatures of the first compartment 11A and the second compartment 11B in the reaction vessel 11.
As shown in Table 1, in this example, the waste liquid is rendered harmless under the conditions of a pressure of 10 MPa in the reaction vessel, a residence time of 53 s in the reaction vessel, a waste liquid flow rate of 20 kg / h, and an air flow rate of 2.9 kg / h. I was able to.
In the first section 11A, the temperature of the fluid that flowed in could be increased from 340 ° C. to 440 ° C. without turning on the heater.
This is because the heat due to the oxidative decomposition of the second section 11B has moved to the first section 11A. At this time, the average temperature of the second section 11B was 450 ° C.

The embodiments and examples of the present invention have been described above, but the present invention is not limited to the embodiments and examples, and various modifications can be made within the scope of the gist of the present invention described in the claims. Can be modified or changed.
For example, although the partition member has a cylindrical shape in each of the above embodiments, the same effect can be obtained even when it is a single plate shape.
The effects described in the embodiments of the present invention are merely examples of the most preferable effects resulting from the present invention, and the effects of the present invention are limited to those described in the embodiments of the present invention. is not.

DESCRIPTION OF SYMBOLS 10 Reactor 11A 1st division 11B 2nd division 11D Solid substance storage division 12 Partition member 18, 32 Fin 27, 29 as a member which has heat conductivity Catalyst 34 Plate as a member which has heat conductivity

Japanese Patent No. 3437737

Claims (8)

A reactor that decomposes the organic matter by an oxidation reaction in a state where the object to be treated containing the organic matter and the oxidizing agent are mixed or introduced separately, and the water becomes supercritical water, superheated steam, or subcritical water; ,
The reactor is provided so as to extend from one end side toward the other end side, and a first compartment into which the object to be treated and the oxidizing agent are introduced is discharged from the reactor, and the treated fluid is discharged. A partition member divided into a second compartment having a discharge port to be
With
The partition member is configured so that the mixed fluid of the first compartment flows from the one end side toward the other end side, and is folded at the other end side to flow in the second compartment in a direction opposite to the first compartment. Arranged,
The waste liquid processing apparatus which has the structure which controls a heat transfer so that the heat of a 2nd division may move to the 1st division via the said partition member. The waste liquid treatment apparatus according to claim 1,
A waste liquid treatment apparatus in which the structure for controlling the heat transfer is made wider than the original heat transfer area on the first compartment side by changing the shape. The waste liquid treatment apparatus according to claim 2,
A waste liquid treatment apparatus in which the structure for controlling heat transfer is made wider than the original heat transfer area by adding a member for improving heat transfer. The waste liquid treatment apparatus according to claim 2,
A waste liquid treatment apparatus, wherein the partition member is cylindrical, and the partition member has a bent or uneven shape. In the waste liquid processing apparatus as described in any one of Claims 1-4,
The reactor is a vertical type in which the one end side is an upper side and the other end side is a lower side, and the other end side is a solid matter storage compartment in which inorganic solid matter precipitated during processing settles and accumulates. A waste liquid treatment device. In the waste liquid processing apparatus according to any one of claims 1 to 5,
A waste liquid treatment apparatus comprising a catalyst for promoting oxidative decomposition of the object to be treated in at least a second compartment. The waste liquid treatment apparatus according to claim 6,
The catalyst includes one or more of Ru, Pd, Rh, Pt, Au, Ir, Os, Fe, Cu, Zn, Ni, Co, Ce, Ti, and Mn as active species. Waste liquid treatment equipment. In the waste liquid processing apparatus as described in any one of Claims 1-7,
The partition member is made of Fe, Ni, Ti, Ta, Cu, Ag, Au, Pt, Ir, Rh, Pd, Al, Cr, or an alloy that combines two or more of these. .

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