JP4156761B2 - Batch supercritical water reactor - Google Patents

Description

[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a batch-type supercritical water reactor, and more specifically, a batch in which an object to be treated is completely supercritical water treated so that it is easy and safe to operate and no undecomposed product is generated. The present invention relates to a supercritical water reactor.
[0002]
[Prior art]
With increasing awareness of environmental issues, attention has been paid to attempts to decompose and detoxify environmental pollutants using supercritical water reactions with high oxidation and decomposition capabilities of organic matter. That is, due to the supercritical water reaction utilizing the high reactivity of supercritical water, harmful and hardly decomposable organic substances that have been difficult to be decomposed by the prior art, such as PCB (polychlorinated biphenyl), dioxin, and organic chlorine It is an attempt to decompose solvents and convert them into harmless products such as carbon dioxide, water and inorganic salts.
As one of the attempts, recently, supercritical water reaction has also been applied to the treatment of various liquid and solid waste such as sewage sludge, municipal waste, industrial wastewater, etc. containing such harmful organic compounds. The use of is being tried.
[0003]
A supercritical water reactor is a device that decomposes organic substances using the high reactivity of supercritical water. For example, it decomposes harmful organic substances that are difficult to decompose and converts them into harmless carbon dioxide and water. In order to decompose difficult-to-decompose high-molecular compounds and convert them into useful low-molecular compounds, their practical application is currently being actively studied.
Supercritical water refers to water in a supercritical state, that is, water in a state exceeding the critical point of water, and more specifically, at a temperature of 374.1 ° C. or higher and a pressure of 22.04 MPa or higher. Says water in a certain state. Supercritical water has a high ability to dissolve organic substances, and can completely dissolve non-polar substances that are abundant in organic compounds. Conversely, the ability to dissolve inorganic substances such as metals and salts is extremely low. Supercritical water can be mixed with a gas such as oxygen or nitrogen at an arbitrary ratio to form a single phase.
[0004]
Here, a basic configuration of a conventional supercritical water reactor will be described with reference to FIG. FIG. 3 is a flow sheet showing the configuration of a conventional supercritical water reactor.
A conventional supercritical water reactor 90 is a device for treating a fine solid water slurry such as sewage sludge by a supercritical water reaction, and as shown in FIG. 3, as a reactor for performing a supercritical water oxidation reaction, A tube-shaped long pressure-resistant sealed reactor 91 is provided. The supercritical water reactor 90 has a preheater 92 that preheats the reaction fluid upstream of the reactor 91, and a heat that cools the reaction product fluid by exchanging heat with the reaction fluid downstream of the reactor 91. An exchanger 93 and a cooler 94 that cools the reaction product fluid with cooling water are provided.
[0005]
Furthermore, the supercritical water reactor 90 has a pressure gauge 96 and a pressure control valve 97 for measuring the pressure in the reactor 91 in the reaction product line 95 downstream of the cooler 94. The pressure in the reactor 91 is controlled by adjusting the pressure control valve 97 by the pressure control device 98 based on the value.
In addition, the supercritical water reactor 90 includes a gas-liquid separator 99 that gas-liquid separates the reaction product fluid into gas and slurry downstream of the pressure control valve 97, and further separated by the gas-liquid separator 99. A solid-liquid separator 100 is provided for solid-liquid separation of the slurry-like reaction product to separate inorganic solids from the reaction product.
The inorganic solid separated by the solid-liquid separator 100 is mainly contained in the reaction product and has not contributed to the reaction, and may further contain a salt generated by the supercritical water oxidation reaction. is there.
[0006]
The preheater 92 includes an inner tube through which a reaction product composed of an organic substance containing inorganic solids to be processed by a supercritical water reaction, such as sewage sludge, and oxidant air, and an outer tube through which a heating medium for heating the reaction product flows. It is comprised as a double pipe type heat exchanger consisting of.
The reactor 91 is a tube-like long reactor in order to secure the reaction time of the supercritical water reaction with respect to the reactant, and the supercritical water region is formed by retaining supercritical water in the entire region. is doing. The reaction fluid preheated to the reaction temperature enters the reactor 91 from the reactor inlet close to the preheater 92, undergoes supercritical water reaction, and flows out from the reactor outlet as a reaction product fluid.
[0007]
The heat exchanger 93 is a cooler as a double tube heat exchanger composed of an inner tube through which a reaction product fluid flowing out from the reactor 91 flows and an outer tube through which a heat medium heated by the reaction product fluid flows. 94 is configured as a double-tube heat exchanger composed of an inner tube through which the reaction product fluid cooled through the heat exchanger 93 flows and an outer tube through which a refrigerant body that cools the reaction product fluid flows. ing.
The outer tube of the heat exchanger 93 and the outer tube of the preheater 92 are heated so that the heat medium heated by the reaction product fluid in the heat exchanger 93 enters the preheater 92 and preheats the reactant fluid. It is connected by a pipe 101.
[0008]
A liquid line 102 to be treated for feeding a reactant fluid, for example, sewage sludge, is connected to the inner pipe of the preheater 92, and an air line for feeding an oxidizing agent, for example, air, for oxidizing the organic matter to the liquid line 102 to be treated. 103 merges.
The sewage sludge is pressed into the liquid line 102 and the air line 103 by the sewage sludge pump 104 and the air by the air compressor 105, respectively.
The reactant fluid composed of sewage sludge and air is preheated to the start temperature of the supercritical water oxidation reaction by the preheater 92, then enters the reactor 91, and flows through the reactor 91 from the inlet to the outlet. The organic matter in the physical fluid is mainly converted into water, nitrogen, and carbon dioxide by the supercritical water reaction, and flows out from the reactor 91 as a reaction product. The length of the reactor 91 is determined so as to cover the heating from the reaction start temperature to the reaction temperature with the oxidation heat of the organic matter in the sewage sludge, and then to have the time necessary for the complete decomposition reaction. The reaction product fluid enters the inner tube of the heat exchanger 93, heats the heating medium, cools itself, then flows into the inner tube of the cooler 94, and is cooled by the refrigerant body, for example, cooling water, and flows out. .
[0009]
A reaction product line 95 is connected to an outlet of the inner pipe of the cooler 94, and is connected to a gas-liquid separator 99 via a pressure control valve 97.
In the gas-liquid separator 99, the reaction product is gas-liquid separated and separated into a gaseous reaction product and a slurry-like reaction product. The gaseous reaction product is released into the atmosphere or moves to the next processing step, and the slurry reaction product is introduced into the solid-liquid separator 100. The slurry-like reaction product is solid-liquid separated into a liquid processing liquid and an inorganic solid by the solid-liquid separator 100, and each is sent to the outside.
[0010]
[Problems to be solved by the invention]
By the way, the supercritical water reactor that has been put into practical use is a continuous reactor as described above, and is a practical batch type supercritical water reactor except for experimental devices such as bench scales. At present, this has not been realized due to various technical problems.
On the other hand, the objects to be treated with supercritical water are various in accordance with the spread of environmental pollution in recent years, and contaminated solids and contaminated soil that cannot always be treated with a continuous reactor. There is also a need to deal with.
[0011]
When processing a solid substance with a continuous reactor, it is necessary to pulverize the contaminated solid substance into a slurry. However, some of the contaminated solid substance is technically difficult to pulverize.
Even if the contaminated solid material can be pulverized into a slurry, there are the following problems inherent to the slurry.
Firstly, since the pulverized solid is separated by settling or floated, it is often difficult to stably feed the solid water slurry into the continuous reaction apparatus.
Secondly, when the solid material is processed, the inorganic material contained in the solid material does not affect the supercritical water reaction as described above. Therefore, it is important for the continuous operation to flow out together with the processing liquid. However, in a continuous reaction apparatus, it is not easy to discharge inorganic substances or inorganic salts derived from inorganic substances.
Thirdly, there is a problem that a special device is required as a device for handling the slurry, there is no commercial product, and further, the device for handling the slurry is severely damaged, and there is a problem in terms of economy because of the short life.
[0012]
In view of this, it is necessary to feed the objects to be treated into a reactor in a batch manner and perform a batch-type supercritical water treatment.
In addition, since the batch reactor opens the reaction vessel for each batch, it has an excellent advantage that residual inorganic substances or inorganic salts can be easily discharged.
In view of the above situation, an object of the present invention is to provide a batch supercritical water reactor that is easy to operate and practical.
[0013]
[Means for Solving the Problems]
As a result of studying technical problems that could not realize a practical batch-type supercritical water reactor, the present inventor has found that the problems are summarized in the following items.
The first problem is that under supercritical water reaction conditions, such as a temperature of 600 ° C. and a pressure of 25 MPa, the density of supercritical water is about 0.07 g / cm 3.^ThreeHowever, it is remarkably small compared with normal water. Therefore, if processing object, water, oxidizer, auxiliary fuel, etc. are put into the reactor from the beginning, a very large reaction vessel is required. As a result, the equipment cost increases, and the economical efficiency of the apparatus becomes a problem.
[0014]
Secondly, in the batch type supercritical water treatment in which solids are treated, if the amount of solids to be filled is too large, the reaction temperature and reaction pressure of the reactor become too high. There is a problem related to the first problem that the filling amount of the solid object to be processed must be limited.
[0015]
The third problem is that it is difficult to accurately determine the quantitative balance between the object to be treated and water to be introduced into the reactor. As a result, as described below, it is difficult to control the reaction temperature.
The oxidation reaction start temperature is TS, the supercritical water oxidation reaction temperature is TR, the mass of the reactor is Wkg, and the masses of the processing object, water, and oxygen gas charged into the reactor are Xkg, Ykg, and Zkg, respectively. In addition, the average specific heat of the reactor constituent members is Cpwkcal / kg ° C., and the average specific heat of the processing object, water, and oxygen gas charged into the reactor is Cpxkcal / kg ° C., Cpykcal / kg ° C., and Cpzkcal / kg ° C., respectively. The calorific value per unit mass of the object to be treated is Hkcal / kg.
The total calorific value XH of the object to be processed is in the relationship of the following formula with the above-mentioned factors. Where q is the amount of heat released from the reactor.
XH = (Y.Cpy + X.Cpx + Z.Cpz + W.Cpw) (TR-TS) + q
[0016]
Therefore, if the heat cannot be dissipated so as to satisfy the above formula, the temperature in the reactor rises and there is a high risk of runaway reaction. In other words, it is difficult to control the temperature in the reactor. Further, in order to increase the amount X of the solid object to be processed using the same reactor, it is necessary to increase the heat release amount q.
However, in batch supercritical water reactors, there are few means for controlling the progress of the reaction from the outside, and the temperature inside the reactor is mainly left to the supercritical water reaction, so the temperature inside the reactor must be controlled. Is extremely difficult technically.
[0017]
Fourth, as the supercritical water reaction proceeds, CO₂Gas or N₂Gas etc. are generated, the pressure in the reactor rises, and its control is difficult.
[0018]
Accordingly, the present inventor has provided a semi-batch type supercritical water reactor as a first problem, and a second problem is that a relatively large amount of solids is pretreated in a batch type in the first reactor. It was decided to solve the problem by subjecting the reaction product fluid containing the undecomposed matter discharged from the first reactor to the supercritical water treatment in the second reactor.
The third problem is that the temperature of the treatment liquid flowing out of the reactor is measured, and the temperature of the reactor is controlled by adjusting the flow rate of the oxidizing agent based on the temperature. The point is generated CO₂Gas or N₂The inventors have conceived to solve each problem by causing gas and the like to flow out together with the processing liquid, and have repeated experiments to complete the present invention.
[0019]
In order to achieve the above object, based on the above knowledge, the batch type supercritical water reactor according to the present invention is openable and closable, accommodates an object to be treated, and performs batch type supercritical water treatment. One reactor,
Water supply means for supplying supercritical water to the first reactor;
First oxidant feeding means for feeding oxidant into the first reactor;
A continuous second reactor which flows in the first reaction product fluid containing undecomposed matter flowing out from the first reactor and further performs supercritical water treatment;
A second oxidant feeding means for feeding the oxidant into the second reactor;
It is characterized by having.
[0020]
In the present invention, the supercritical water and the oxidant are fed by the water feeding means and the first oxidant feeding means, and the supercritical water treatment is performed on the processing object accommodated in the first reactor. A first reaction product fluid containing the reaction product of the water reaction flows out of the first reactor.
In the first reactor, since it is difficult to completely terminate the supercritical water reaction, the first reaction product fluid flowing out of the first reactor tends to contain undecomposed matter. In the present invention, the undecomposed product refers to a substance that is further decomposed by supercritical water treatment to generate nitrogen, carbon dioxide, acid, water, etc., and is often an environmentally harmful component. .
Therefore, a second reactor connected in series to the first reactor is provided, and the reaction product fluid containing undecomposed matter flowing out from the first reactor is finally completely treated with supercritical water in the second reactor. Thus, without making the reaction conditions of the supercritical water treatment in the first reactor harsh, the first reactor can be filled with a relatively large amount of solids and completely supercritical water treated.
[0021]
In a preferred embodiment of the present invention, a first thermometer for measuring the temperature of the first reaction product fluid;
The first oxidant feed flow rate of the first oxidant feed means is adjusted based on the temperature measured by the first thermometer to control the temperature of the first reaction product fluid to the target temperature. A temperature control device;
A second thermometer for measuring the temperature of the second reaction product fluid flowing out from the second reactor, and an oxidant feed flow rate of the second oxidant feed means based on a temperature measurement value by the second thermometer. And adjusting the temperature of the second reaction product fluid so that the temperature of the second reaction product fluid becomes the target temperature;
It has.
[0022]
In this embodiment, as described above, the temperature of the reaction product fluid flowing out from the first and second reactors is measured, and the flow rate of the oxidant is adjusted based on the temperature, whereby the first and second oxidants are adjusted. The reactor temperature is controlled.
[0023]
Preferably, neutralization quenching means for feeding the second reaction product fluid with an alkaline aqueous solution and neutralizing and quenching the second reaction product fluid is provided at an appropriate position.
Thereby, when the second reaction product fluid is acidic, corrosion of the cooling means, gas-liquid separation means, liquid feeding means, etc. due to the second reaction product fluid can be prevented.
[0024]
Practically, the batch supercritical water reactor according to the present invention includes a cooling means for cooling the second reaction product fluid,
Gas-liquid separation means for gas-liquid separation of the cooled second reaction product fluid;
A liquid feeding means for feeding the liquid component obtained by gas-liquid separation by the gas-liquid separation means to the water feeding means to form at least a part of supercritical water;
In place.
As a result, a closed system can be configured for the liquid, so that environmental pollution due to drainage or the like does not occur.
Moreover, when neutralizing a 2nd reaction product fluid with an alkaline agent, the liquid feeding means is equipped with the inorganic salt separation apparatus which isolate | separates the inorganic salt in the liquid component to send.
As long as the inorganic salt separation device can separate the inorganic salt in the liquid component, for example, an ion exchange resin device can be suitably used regardless of the type and type.
[0025]
DETAILED DESCRIPTION OF THE INVENTION
Embodiments of the present invention will be described below specifically and in detail with reference to the accompanying drawings.
Embodiment 1
This embodiment is an example of an embodiment of a batch supercritical water reactor according to the present invention, and FIG. 1 is a flow sheet showing the configuration of the batch supercritical water reactor of this embodiment.
The batch type supercritical water reaction apparatus 10 (hereinafter referred to as the reaction apparatus 10) of the present embodiment is an apparatus that treats organic solids that are difficult to pulverize in a batch type by a supercritical water reaction.
As shown in FIG. 1, the reactor 10 flows in a first reactor 12 that performs batch-type supercritical water treatment, and a first reaction product fluid that has flowed out of the first reactor 12 and contains undecomposed matter. In order to perform further supercritical water treatment, a continuous second reactor 14 connected in series to the first reactor 12, and a water feeding means 16 for feeding supercritical water into the first reactor 12, The air compressor 18 that feeds air as an oxidant into the first reactor 12 and the second reactor 14, and the reaction product that cools the second reaction product fluid that has flowed out of the second reactor 14 and separates the gas and liquid A material outflow system 20 is provided.
[0026]
The first reactor 12 is an openable / closable autoclave-type reactor that accommodates an object to be treated and performs supercritical water treatment, and supports the object to be treated inside the reactor, It has a plate-like support plate 21 that allows supercritical water to pass through, and an inner cylinder 22 that is held in one place so that the object to be treated on the support plate 21 is not dispersed.
The second reactor 14 is a continuous reactor connected to the first reactor outlet pipe 24 of the first reactor 12 and may be a tube type or a container type.
The water supply means 16 includes a water tank 26 that stores water, a water pump 28 that supplies the water stored in the water tank 26, and a heating furnace 30 that heats the water supplied by the water pump 28. Supercritical water is sent to the first reactor 12 via 32.
[0027]
The air compressor 18 is a compressor of a type that can easily control the air flow rate by adjusting a flow rate control valve provided in the discharge pipe, and is provided with a first air supply pipe 34 and a water supply pipe 32. Then, air is fed as an oxidant to the first reactor 12 and to the second reactor 14 via the second air supply pipe 36 and the first reactor outlet pipe 24, respectively.
The inlet flow rate of the air compressor 18 is adjusted by a temperature control device based on the temperature of the reaction product fluid, as will be described below.
That is, the reactor 10 adjusts the amount of air sent to the first reactor 12 and the second reactor 14 to control the temperature in the first reactor 12 and the temperature in the second reactor, respectively. The first temperature control device 38 and the second temperature control device 40 are provided.
[0028]
The first temperature control device 38 is provided in the first air supply pipe 34 provided on the discharge side of the air compressor 18 based on the temperature measurement value of the first thermometer 42 provided in the first reactor outlet pipe 24. The flow rate of the air fed into the first reactor 12 is adjusted by adjusting the valve opening degree of the 1 flow rate adjusting valve 44, and the temperature in the first reactor 12 is controlled to a predetermined temperature.
That is, when the temperature measurement value of the first thermometer 42 is higher than the predetermined temperature, the flow of air is decreased to suppress the progress of the supercritical water reaction in the first reactor 12, and the temperature measurement of the first thermometer 42 is performed. When the value is lower than the predetermined temperature, the air flow rate is increased to promote the progress of the supercritical water reaction. Usually, the target temperature of a 1st reactor is about 500-550 degreeC.
[0029]
The second temperature control device 40 is based on the temperature measurement value of the second thermometer 48 provided in the second reactor outlet pipe 46, and the second temperature control device 40 is provided in the second air supply pipe 36 on the discharge side of the air compressor 18. The flow rate of the air sent into the 2nd reactor 14 is adjusted by adjusting the valve opening degree of 2 flow control valve 50, and the temperature in the 2nd reactor 14 is controlled to predetermined temperature.
That is, when the temperature measurement value of the second thermometer 48 is higher than the predetermined temperature, the flow rate of air is decreased to suppress the progress of the supercritical water reaction, and when the temperature measurement value of the second thermometer 48 is lower than the predetermined temperature. Increase the air flow rate to complete the supercritical water reaction. The target temperature of the second reactor 14 is about 600 to 650 ° C., and auxiliary fuel may be supplied from the outside as necessary.
[0030]
The reaction product outflow system 20 is provided in the second reactor outlet pipe 46 that allows the fluid to flow out from the second reactor 14, and includes a cooler 52 that cools the reaction product fluid that has flowed out of the second reactor 14, A gas-liquid separator 54 provided downstream of the reactor 52, and a pressure control device 56 for controlling the pressure of the gas-liquid separator 54, and thus indirectly the pressure of the second reactor 14 and further of the first reactor 12, And a liquid level controller 58 for controlling the liquid level of the gas-liquid separator 54.
[0031]
The gas-liquid separator 54 gas-liquid separates the second reaction product fluid flowing out from the second reactor 14 and separates it into a gas component and a water component. The gas component is discharged to the atmosphere through a gas discharge pipe 60 connected to the top of the gas-liquid separator 54.
The pressure control device 56 adjusts the valve opening degree of the pressure control valve 64 based on the measurement value of the pressure gauge 62 provided in the gas discharge pipe 60, and controls the pressure of the gas-liquid separator 54 to be a predetermined pressure. To do.
The first reactor outlet pipe 24 is provided with a CO concentration meter 66 for measuring the CO gas concentration in the gas component. A CO concentration meter 67 may also be provided in the gas discharge pipe 60.
[0032]
The liquid level control device 58 controls the liquid level of the gas-liquid separator 54 by adjusting the valve opening degree of the flow rate adjusting valve 70 provided in the liquid outflow pipe 68 through which the water component flows out from the gas-liquid separator 54. .
[0033]
Furthermore, the reaction apparatus 10 includes equipment for injecting an alkaline aqueous solution into the second reactor outlet pipe 46. The alkaline aqueous solution injection facility includes an alkaline aqueous solution tank 72, an alkaline aqueous solution pump 74, and an alkaline aqueous solution injection pipe 76 connected to the second reactor outlet pipe 46. The aqueous solution is pumped and injected into the second reactor outlet pipe 46 via the alkaline aqueous solution injection pipe 76. By injecting the alkaline aqueous solution, the second reaction product fluid can be neutralized and rapidly cooled.
In particular, when the second reaction product fluid that has flowed out of the second reactor 14 is acidic, it is preferable to neutralize it by injecting an alkaline aqueous solution and quench it.
[0034]
Next, a method for operating the batch supercritical water reactor 10 of the present embodiment will be described with reference to FIG.
First, the first reactor 12 is opened, the processing target for one batch operation is placed on the support plate 21 in the inner cylinder 22, and the first reactor 12 is closed. When the object to be treated is a slurry fluid, the first reactor 12 can be filled as it is through the water supply pipe 32 without opening the first reactor 12.
Next, the water supply pump 28 is activated to supply water from the water tank 26 to the heating furnace 30 through the water supply pipe 32, heated and supplied to the first reactor 12.
The water flowing out from the first reactor 12 enters the gas-liquid separator 54 through the second reactor 14 and the cooler 52. Next, the water extracted from the gas-liquid separator 54 is combined with the water from the water pump 28 by a circulation means (not shown), heated in the heating furnace 30 and put into the reactor 12, and the circulation is gradually started.
As the amount of circulating water increases, the amount of water supplied by the water supply pump 28 is decreased, and finally the amount of water flowing out of the system together with the gas from the gas discharge pipe 60 is replenished by the water supply pump 28.
[0035]
When the temperature measured by the first thermometer 42 reaches 370 ° C., the air compressor 18 is started and air is sent to the first reactor 12 via the first air supply pipe 34 and the water supply pipe 32. Enter. In order to keep the system pressure constant, the air compressor 18 may be operated from the start-up. Further, both the first reactor and the second reactor can be heated to a predetermined temperature by a heating means such as an electric furnace installed outside. In this case, heating medium heating or the like can be used as the external heating means in addition to the electric furnace.
Next, the first temperature control device 38 is operated to adjust the valve opening of the first flow rate control valve 44 so that the temperature measured by the first thermometer 42 becomes a predetermined temperature, and the first reactor 12 is adjusted. Adjust the amount of air sent to the.
[0036]
When the conditions in the first reactor 12 reach the supercritical water reaction conditions, the supercritical water reaction is started and gradually proceeds. Since undecomposed matter remains in the first reaction product fluid flowing out from the first reactor 12, supercritical water treatment is further performed on the first reaction product fluid in the second reactor.
When the decomposition target contains inorganic salts, the first reactor 12 is heated to a critical temperature or higher in advance by an external heating means in order to prevent the inorganic salts from dissolving and flowing into the second reactor 14. It is possible to cause water to flow into the first reactor 12 later.
As the supercritical water reaction proceeds, the fluid flowing out from the second reactor outlet pipe 46 is a gas component such as CO2.₂The gas is entrained, cooled by the cooler 52, separated by the gas-liquid separator 54, and discharged through the gas discharge pipe 60 under the control of the pressure control device 56.
[0037]
When the CO gas concentration in the CO gas concentration meter 66 provided in the first reactor outlet pipe 24 is not detected, it can be determined that the supercritical water reaction in the reactor 12 has reached the end point.
In addition, when a TOC analyzer (not shown) is provided in the first reactor outlet pipe 24 and the TOC concentration in the TOC analyzer is not detected, the supercritical water reaction in the first reactor 12 is similarly terminated. It can be determined that it has been reached. When the measured value of either the CO gas concentration meter 66 or the TOC analyzer reaches a certain value, it can be determined that the supercritical water reaction in the first reactor 12 has reached the end point. It is more reliable to determine the end point when the measured value reaches a certain value. In addition, it is preferable to confirm that there is no CO gas in the released gas by a CO concentration meter 67 provided in the gas releasing pipe 60.
When the supercritical water reaction reaches the end point, the pressure of the entire batch supercritical water reactor 10 is reduced, and then the first reactor 12 is opened.
Even if the CO gas concentration meter 66 or the TOC analyzer is not installed in the first reactor outlet pipe 24, a reaction test can be performed in advance separately using a small basic tester, and the reaction end time can be predicted from the result.
[0038]
Embodiment 2
This embodiment is another example of the embodiment of the batch supercritical water reactor according to the present invention, and FIG. 2 is a flow sheet showing the configuration of the batch supercritical water reactor of this embodiment. is there.
The batch type supercritical water reactor 80 (hereinafter referred to as the reactor 80) of the present embodiment is an apparatus that batch-processes organic solids that are difficult to grind by supercritical water reaction, as in the first embodiment. is there.
As shown in FIG. 2, the reactor 80 includes an inorganic salt separation device 82 that separates inorganic salts from water components flowing out from the gas-liquid separator 54. Except for using as water, it has the same configuration as the first embodiment.
[0039]
As shown in FIG. 2, the main part of the reaction apparatus 80 includes a booster pump 84 in the liquid outflow pipe 68 upstream of the flow rate control valve 70, and converts the water component in the gas-liquid separator 54 to the inorganic salt separation apparatus 82. Then, after the inorganic salt is separated there, it is further sent to the water supply pipe 32 through the circulation pipe 86.
The inorganic salt separation device 82 is a device for separating an inorganic salt in a liquid, and is, for example, an ion exchange resin device.
[0040]
The operation of the reactor 80 of the present embodiment is the same as that of the reactor 10 of the first embodiment, and is performed by the gas-liquid separator 54 via the booster pump 84, the inorganic salt separator 82 and the circulation pipe 86. The separated water component is circulated to the water supply pipe 32.
[0041]
In Embodiments 1 and 2, the first reactor outlet pipe 24 connects the bottom of the first reactor 12 and the top of the second reactor 14, but the first reactor 12 and the second reaction are connected. The connection method with the reactor 14 is not necessarily limited to this. For example, the first reactor outlet pipe is connected to the second portion connected to the annular portion of the outer wall of the first reactor 12 and the inner cylinder 22 and the second portion. The top of the reactor 14 may be connected.
[0042]
【The invention's effect】
According to the present invention, by providing a batch reactor for performing supercritical water treatment and a continuous reactor downstream of the batch reactor, the object to be treated is supercritically treated by the batch reactor. The water can be treated and then completely supercritical water treated by a continuous reactor so that no undecomposed product remains.
Further, based on the temperature measurement value of the first reaction product fluid, the temperature control device adjusts the flow rate of the oxidizing agent to the first reactor so that the fluid temperature becomes the target temperature. By controlling the temperature in the reactor, a batch supercritical water reactor that is easy to operate and safe is realized.
Furthermore, a gas-liquid separator that gas-liquid separates the fluid flowing out from the reactor is provided in the reactor outflow system, and the separated liquid is heated and then sent to the reactor as at least part of supercritical water. Establish a circulation path and facilitate batch operation.
[Brief description of the drawings]
FIG. 1 is a flow sheet showing the configuration of a batch supercritical water reactor according to Embodiment 1;
FIG. 2 is a flow sheet showing the configuration of a batch supercritical water reactor according to Embodiment 2;
FIG. 3 is a flow sheet showing the configuration of a conventional supercritical water reactor.
[Explanation of symbols]
10 Batch-type supercritical water reactor of Embodiment 1
12 First reactor
14 Second reactor
16 Water supply means
18 Air compressor
20 Reaction product outflow system
22 Eyeplate-shaped support plate
24 First reactor outlet pipe
26 Water tank
28 Water pump
30 Heating furnace
32 Water pipe
34 First air supply pipe
36 Second air supply pipe
38 First temperature control device
40 Second temperature control device
42 First thermometer
44 First flow control valve
46 Second reactor outlet tube
48 Second thermometer
50 Second flow control valve
52 Cooler
54 Gas-liquid separator
56 Pressure control device
58 Liquid level control device
60 Gas release pipe
62 Pressure gauge
64 Pressure control valve
66 CO concentration meter
68 Liquid outflow pipe
70 Flow control valve
72 Alkaline aqueous solution tank
74 Alkaline aqueous solution pump
76 Alkaline aqueous solution injection tube
80 Batch-type supercritical water reactor of Embodiment 2
82 Inorganic salt separator
84 Booster Pump
86 Circulation pipe
90 Conventional continuous supercritical water reactor
91 Pressure-resistant sealed reactor
92 Preheater
93 Heat exchanger
94 Cooler
95 Reaction product line
96 Pressure gauge
97 Pressure control valve
98 Pressure control device
99 Gas-liquid separator
100 Solid-liquid separator
101 Heating medium piping
102 Liquid line to be treated
103 Air line
104 Sewage sludge pump
105 Air compressor

Claims (5)

A first reactor that is openable and closable, contains a processing object, and performs batch-type supercritical water treatment;
Water supply means for supplying supercritical water to the first reactor;
First oxidant feeding means for feeding oxidant into the first reactor;
A continuous second reactor which flows in the first reaction product fluid containing undecomposed matter flowing out from the first reactor and further performs supercritical water treatment;
A batch type supercritical water reactor comprising a second oxidizing agent feeding means for feeding an oxidizing agent into the second reactor. A first thermometer for measuring the temperature of the first reaction product fluid;
The first oxidant feed flow rate of the first oxidant feed means is adjusted based on the temperature measured by the first thermometer to control the temperature of the first reaction product fluid to the target temperature. A temperature control device;
A second thermometer for measuring the temperature of the second reaction product fluid flowing out from the second reactor, and an oxidant feed flow rate of the second oxidant feed means based on a temperature measurement value by the second thermometer. 2. A batch type supercritical water reactor according to claim 1, further comprising: a second temperature control device that controls the temperature of the second reaction product fluid to be a target temperature by adjusting the temperature of the second reaction product fluid. . A neutralization and quenching means for neutralizing and quenching the second reaction product fluid by feeding an alkaline aqueous solution into the second reaction product fluid is provided downstream of the second reactor in claim 1, and in claim 2. In such a case, the batch type supercritical water reactor is provided downstream of the second thermometer. Cooling means for cooling the second reaction product fluid;
Gas-liquid separation means for gas-liquid separation of the cooled second reaction product fluid;
The liquid feeding means for feeding the liquid component obtained by gas-liquid separation by the gas-liquid separation means to the water feeding means to make at least a part of supercritical water is the second reactor of claim 1. A batch type supercritical water reaction apparatus provided downstream of the second thermometer according to claim 2 and downstream of the neutralization quenching means according to claim 3. The batch type supercritical water reactor according to claim 4, wherein the liquid feeding means includes an inorganic salt separation device for separating an inorganic salt in a liquid component to be fed.

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