JPH11290872A - Supercritical hydroxylation treatment system of organic matter and its operation - Google Patents

Abstract

PROBLEM TO BE SOLVED: To achieve the enhancement of an energy rocovery ratio, the reduction of running cost and the miniatirization of a preheater. SOLUTION: The fluid 102 subjected to oxidation reaction in a reactor 1 is sent to a preheater 2b to be heat-exchanged with a fluid 101 before reaction and subsequently separated into a gaseous phase and a liquid phase by gas-liquid separation 4 and the gaseous phase 104 is used in the generation of electricity while the liquid phase 105 is used in the driving of a hydraulic pressure drive pump 10 and guided to a preheater 2a to be heat-exchanged with the fluid before reaction. When a gas turbine 5 is driven by exhaust gas 104, the exhaust gas is heated by a combuster 13 and an exhaust gas heater 12 and a part of the fluid 105 is sent to an oxygen preheater 26 not only to preheat liquid oxygen 103 but also to perform the generation of electricity by using a thermoelectric converter element 44. The energy possessed by a fluid 102 after reaction is sufficiently recovered and the power required in the driving of a pump 8 or the like is provided by the generation of electricity generated in this system to suppress the consumption of oxygen 103.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a processing system suitable for oxidizing organic substances in a supercritical fluid using water as a solvent and a method of operating the same.

[0002]

2. Description of the Related Art With respect to purification treatment of household wastewater and industrial wastewater containing organic substances, a method utilizing a decomposition reaction by microorganisms is widely used. When this method is used, a large amount of sludge is generated with the treatment. The generated sludge is disposed of by incineration or landfill. However, if the sludge is reclaimed as it is, the amount of sludge will be a problem,
Many perform incineration.

[0003] For incineration of sludge, a method using an incinerator is currently most popular, as in general incineration. However, in order to make the sludge flammable, the proportion of non-combustible substances such as inorganic components and moisture in the sludge is required. It is necessary to take measures such as reducing fuel consumption or adding fuel to support the combustion of sludge. Since the water content of sewage sludge reaches 97 to 98% by mass, a method of concentrating and dewatering the sludge to reduce the water content to about 80% and then supplying it to an incinerator is widely used. I have.

A method called a wet oxidation method has been proposed as an alternative method. This method uses 200
Air or oxygen is forcibly sent as an oxidizing agent at a temperature of about 300 ° C. and a hot water condition of about 100 atm.
It causes an oxidative decomposition reaction. This method has an advantage in that the sludge can be oxidized in the presence of water as compared with the method using an incinerator, so that pretreatment such as reducing the amount of water in the sludge can be simplified. Further, there is an advantage that generation of harmful gas as seen in a general incinerator can be suppressed, and an exhaust gas treatment device is not required.
However, this method has a problem that the decomposition level does not increase for organic substances that are difficult to decompose.

As a method for improving the problem with respect to the decomposition level, a supercritical water oxidation method in which an oxidation reaction is caused under supercritical conditions of water has recently attracted attention, and as an example, Japanese Patent Application Laid-Open No. 6-511190. There is a disclosed technology. In this method, a mixture of organic matter, oxygen and water is brought to a supercritical condition of water (22 MPa or more, 374 ° C. or more),
The mixed fluid becomes a supercritical state, and organic matter is immediately oxidized. In water in a supercritical state, the organic substance and oxygen are mixed uniformly in the same phase, so that the reaction speed is high and the property is close to complete combustion.

[0006]

In the above-mentioned supercritical water oxidation method for water, it is necessary to pressurize and heat the treatment fluid to the supercritical condition of water, so that energy for operating the whole system is required. There is a disadvantage in terms of increased consumption and cost. As a method of solving this, means for recovering energy from a fluid that has reacted in a supercritical state can be considered. As an example, there is a technique disclosed in Japanese Patent Publication No. 1-38532.
As a means for recovering energy in a wet oxidation treatment in a subcritical state, there is a technique disclosed in Japanese Patent Application Laid-Open No. 62-142811. However, the method of performing energy recovery after processing in a subcritical state cannot be applied to a fluid in a supercritical state where there is no distinction between a gaseous phase and a liquid phase in the fluid after the reaction. Also, in the technology disclosed in Japanese Patent Publication No. 1-38532 for recovering energy from a supercritical state,
Since water flows into the turbine at a time when it is in a supercritical state, it is separated into two phases of gas and liquid in the turbine, and as a result, the fluid must be released at a high pressure, so that energy recovery is not sufficient.

As a means for recovering thermal energy from the fluid after the reaction, the technique disclosed in Japanese Patent Publication No. 1-38532 discloses a method of mixing the fluid after the reaction with the fluid before the reaction. However, if this method is applied to sludge with a relatively high moisture content, the calorific value relative to the heat capacity of the fluid will decrease, and it will not be possible to maintain the supercritical state only with the heat generated by the oxidation reaction, and self-sustaining operation will become impossible. Can not.
Japanese Patent Application Laid-Open No. 6-511190 discloses a method of applying heat from a fluid after a reaction to a fluid before a reaction using a heat medium. Heat exchanger in this case (= preheater)
Must be very large in order to secure the necessary heat exchange capacity. This is because a fluid containing a high concentration of organic matter, such as sludge, generally has a high viscosity, becomes laminar when flowing through a preheater, and has a very poor heat transfer coefficient. Large preheaters increase equipment costs and pump work.

Further, when the processing system is started, a heating unit is required by inputting energy from the outside. As a method for this, a part of the preheater is used for external heating or the fluid after the reaction is heated. Had to tell the fluid before the reaction. The use of a part of the preheater for external heating not only does not work during a steady operation but also causes a pressure loss, thereby increasing the pump load. The method of heating the fluid after the reaction is based on the required amount of heat of 2
There is a problem because it uses twice as much energy.

Further, when air is used as the oxidizing agent,
The work to pressurize this to the pressure of supercritical conditions is large,
Further, since the cost increases when pure oxygen is used, there is a demand for a method of controlling the cost and controlling the cost at a low cost. As one method for solving this problem, the present inventors have previously filed Japanese Patent Application No. 9-303951, which discloses a method in which a fluid after a reaction and a fluid before a reaction flowing through a preheater are heated through a heat transfer surface of the preheater. By exchanging the heat, we proposed a method that enables heat recovery with a small heat transfer surface, reduces the size of the preheater, and reliably performs oxidation while reducing running costs. However, a sufficiently usable heat energy is still left in the fluid after the reaction by such heat exchange, and the conventional heat energy recovery method is not necessarily sufficient in terms of the heat recovery rate.

[0010] The present invention has been made in view of the above problems, and in constructing a supercritical water oxidation treatment system for organic substances, sufficient energy can be efficiently recovered from the fluid after the reaction, and heat recovery is performed. It is an object of the present invention to provide a configuration that does not require a large amount of equipment while allowing independent operation, a configuration that reduces operating costs as a whole, and a method of operating the configuration.

[0011]

In order to achieve the above-mentioned object, the present invention provides an oxidizing reaction between an organic substance and a fluid containing oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance. In an organic matter supercritical water oxidation treatment system that recovers energy from the fluid after the oxidation reaction has been performed, the reacted fluid flows outside the heat transfer tube through which the fluid containing the organic material flows before the reaction. Preheating means that removes the water in the fluid after the reaction from the supercritical state by giving the heat of the fluid after the reaction to the fluid before the reaction, and promotes the reaction by bringing the water in the fluid before the reaction closer to the supercritical state Gas-liquid separation means for separating the fluid after the reaction into a gas component and water,
A supercritical water oxidation treatment system for organic matter, comprising: a gas power generation means for recovering power using the gas component separated by the gas-liquid separation means.

Further, the present invention provides a water-driven pressurizing means for driving a piston with a reacted fluid separated as water by the gas-liquid separating means, and pressurizing a fluid before the reaction with a piston interlocked with the piston. Disclosed is a supercritical water oxidation treatment system for organic matter, wherein the system has a cross-sectional area of a piston in contact with a fluid before the reaction and smaller than a cross-sectional area of the piston in contact with the fluid after the reaction.

Further, the present invention provides a carbon dioxide separating means for separating carbon dioxide from the gas component separated by the gas-liquid separating means, and an oxygen separating means for separating the gas component from which carbon dioxide has been removed by the carbon dioxide separating means. A supercritical water oxidation treatment system for organic matter, comprising: an oxygen separation and recovery means for mixing the separated oxygen with the fluid before the reaction.

The present invention also discloses an organic supercritical water oxidation treatment system comprising an absorption refrigeration unit that operates using the gas component separated by the gas-liquid separation unit as a heat source.

[0015] The present invention further comprises a thermoelectric conversion means for generating electricity by using thermal energy of the fluid after the reaction after passing through the preheating means as a driving source, for supercritical water oxidation of an organic substance. A processing system is disclosed.

Further, the present invention comprises a positive displacement hydraulic motor for recovering power by being driven by the reacted fluid separated as water by the gas-liquid separating means, wherein the supercritical organic substance is supercritical. A hydroxylation treatment system is disclosed.

The present invention further comprises a reflux means for mixing a part of the fluid before the reaction heated by the preheating means with the fluid before the heating by the preheating means. A critical water oxidation treatment system is disclosed.

Further, the present invention further comprises a cooling means for generating a temperature lower than that of the outside air by rapidly expanding the gas component separated by the gas-liquid separation means. An oxidation treatment system is disclosed.

The present invention also discloses a supercritical water oxidation treatment system for organic matter, comprising a heating means for heating water in a fluid before the reaction using electromagnetic induction heating.

Furthermore, the present invention provides a method for oxidizing an organic substance in a supercritical state using water as a solvent and a fluid containing oxygen or an oxidizing agent to oxidize the organic substance. A method of operating a supercritical water oxidation treatment system for organic matter that recovers energy from an organic substance, wherein the oxygen concentration in the gas component of the reacted fluid is measured after the water in the reacted fluid is no longer in a supercritical state. Measuring means, and oxygen or oxidizing agent controlling means for controlling the amount of oxygen or oxidizing agent to be mixed with the fluid containing water and organic matter, wherein the oxygen concentration in the gas component of the fluid after the reaction measured by the oxygen concentration measuring means The organic or oxidizing agent control means controls the amount of oxygen or oxidizing agent to be mixed so that the concentration becomes a predetermined target value. It discloses a method of operating the critical hydroxide treatment system.

[0021]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below in detail with reference to the drawings. FIG. 1 shows a first embodiment of the present invention which solves the conventional problem. The system includes a reactor 1, preheaters 2a and 2b, an oxygen mixer 3, a gas-liquid separator 4, a solid-liquid separator 18, gas turbines 5, 6, pumps 7, 8, a generator 9, a hydraulic drive pump 10, , Combustor 13, exhaust gas heater 1
2. It is composed of a crusher 22, electromagnetic induction heaters 14a and 14b, an oxygen preheater 26, a thermoelectric conversion element 44, an oxygen concentration meter 16, and an oxygen flow controller 17.

The sludge 107 subjected to the dewatering treatment is crushed by the crusher 2
2 and granulated, and then mixed with water 108 in the mixing tank 23 to form the fluid 101. The organic matter concentration in the fluid 101 is controlled by the flow control valves 25 and 24. Since the crushed sludge mixed with water hydrates with the passage of time and increases the viscosity of the sludge fluid 101, the crushed sludge is mixed immediately before being supplied to the oxidation treatment system as shown in FIG. It is appropriate to carry out. The fluid 101 is pressurized to a pressure higher than the critical pressure of water by the pump 8 and the hydraulic pump 10, and is heated by the preheaters 2a and 2b until the supercritical state is reached. The liquid oxygen 103 pressurized by the pump 7 is heated and vaporized by the oxygen preheater 26 and injected into the fluid 101 through the oxygen mixer 3. A fluid in which organic matter and oxygen are mixed in water causes an oxidation reaction in the reactor 1. The fluid 102 after the reaction is processed by the gas-liquid separator 4 and the solid-liquid separator 18, and the energy of the fluid 102 is changed by the preheaters 2 a and 2 b, the gas turbine 5,
6, collected by the hydraulic drive pump 10, the exhaust gas heater 12, the oxygen preheater 26, the thermoelectric conversion element 44 and the like.

The preheater 2a is constituted by a counterflow type double tube heat exchanger, in which the fluid 101 flows on the inner tube side and the reacted fluid 105 flows on the outer tube side. The pressure inside the inner tube may be a pressure at which the fluid 101 does not boil. The electromagnetic induction heaters 14a and 14b are used when there is no high-temperature reacted fluid such as when the system is started. Electromagnetic induction heaters 14a, 1
4b is mounted outside the double tube preheater. Since the inner tube of the double tube of the preheater is made of metal and the outer tube is made of a dielectric, eddy current due to the alternating magnetic field of the electromagnetic induction heater 14 flows only into the inner tube, and flows through the inner tube. Fluid 1
It is convenient to heat 01.

FIG. 11 schematically shows a flow pattern when the fluid 101 flows through the preheater 2a. Crusher 22
As a result, the dewatered sludge 107, which has been granulated to about half the diameter of the heat transfer tube (= inner tube), flows in the fluid 101 as shown in FIG. Rolling of such lumps has the function of reducing the temperature difference between the pipe wall and the center of the pipe, thereby increasing the heat transfer coefficient of the fluid. This improves the performance of the preheaters 2a, 2b.

The temperature of the sludge fluid 101 rises while passing through the preheater 2a, so that the viscosity of the fluid 101 decreases. In addition, the viscosity of the fluid 101 also decreases due to a certain degree of thermal decomposition of the sludge. However, since the sludge has a very high viscosity, the flow in the preheater 2a is only a laminar flow, and the heat transfer coefficient is poor. In order to compensate for this, the diameter of the inner pipe of the double pipe of the preheater 2a is made large, the time required to pass through the heat exchanger by reducing the flow rate is increased, and the time required for the thermal decomposition of the sludge to proceed is increased. Increase the range of viscosity decrease due to decomposition. A part of the fluid whose viscosity has been reduced to some extent by the preheater 2a is returned to a position before the pump 8 and mixed with the fluid before the preheating. Thereby, the viscosity of the fluid can be reduced without changing the concentration, and the pump power can be reduced.

The type of the hydraulic drive pump 10 is shown in FIG.
In FIG. 7, the pressurized fluid 123 is pressurized by the high-pressure fluid 125. The high-pressure fluid 125 is the fluid 1 after the reaction in FIG.
05. The pressure of the pressurized fluid 124 is changed to fluid 1
In order to make the pressure higher than 25, the diameter of the piston on the pressurized fluid side is made smaller than the diameter of the piston on the pressurized fluid side.
In order to operate this pump, a necessary condition is that the volume flow rate of the fluid 125 is larger than the volume flow rate of the fluid 123. However, since the temperature of the fluid 125 is higher than that of the fluid 123, the specific volume is large, and this condition is satisfied. can do.

The preheater 2b is constituted by a double tube heat exchanger like the preheater 2a, and an electromagnetic induction heater 14b is mounted outside thereof. The diameter of the inner tube of the double tube of the preheater 2b is improved in order to improve the heat transfer coefficient and withstand high pressure.
Take smaller than. The sludge fluid 101 reaches a supercritical state or a temperature level close to the supercritical state at the outlet of the preheater 2b.

By mixing oxygen in the oxygen mixer 3 with the preheated fluid 101, an oxidation reaction of organic substances occurs. While the reaction is taking place, the fluid flows through the reactor 1,
Keep insulated from outside. When the fluid temperature rises due to the heat of reaction, the fluid completely enters a supercritical state, and water in the supercritical state becomes an excellent solvent for organic substances. Therefore, the oxidation reaction of organic substances is promoted, and the oxidation reaction proceeds promptly. Will be Sludge components are mainly converted into carbon dioxide, nitrogen and ash by an oxidation reaction. The temperature of the fluid at the outlet of the reactor 1 is higher than the temperature at the inlet of the reactor 1 by the amount of the heat of reaction, and this temperature becomes the maximum temperature. When oxidizing organic matter containing a large amount of nitrogen such as sewage sludge, ammonia may be generated.
It can be suppressed by setting the temperature to a high temperature of 00 to 650 ° C. Increasing the temperature of the fluid before mixing oxygen is most effective for increasing the maximum temperature, and preheating the sludge before mixing oxygen is an effective means.

As oxygen to be mixed, pure oxygen 103 supplied as a liquid is used. The liquid oxygen 103 is pressurized by the pump 7, then vaporized by heating in the oxygen preheater 26, and supplied to the oxygen mixer 3 in a gas (accurately, supercritical state) state. The use of liquid oxygen significantly reduces power as compared to the case of compressing gaseous oxygen. Further, compared with the case where air is added as an oxidizing agent, the nitrogen concentration does not need to be increased, and the generation of ammonia can be suppressed. However, since liquid oxygen is expensive for continuous consumption, the pump 7 is controlled by the oxygen flow controller 17 so as not to consume more than a necessary amount, and control is performed to obtain an optimum oxygen flow rate. .

The fluid 102 exiting the reactor 1 is led to a preheater 2b, where the temperature is lowered by applying heat to the fluid before the reaction. As a result, water as the main component of the fluid 102 changes from a supercritical state to a subcritical state. Since the pressure of the fluid 102 at the outlet of the preheater 2b is equal to the pressure under the critical condition of water, the water in the subcritical state becomes a liquid, and a gas component that is hardly dissolved in water exists in the supercritical state. I do. The gas components mainly consist of carbon dioxide, oxygen and nitrogen. Since the gas component in the supercritical state has a considerably smaller density than water, it can be treated in the same way as gas, and can be separated from water by the gas-liquid separator 4.

The fluid from which the gas components have been removed by the gas-liquid separator 4 is sent to the solid-liquid separator 18 where the solid component as ash is separated. Fluid 105 from which solid components have been removed by solid-liquid separator 18
Is used as a power source for the hydraulic drive pump 10, after which part of the fluid is sent to the preheater 2 a and the other is sent to the oxygen preheater 26. The flow rate of the fluid 105 sent to the preheater 2 a and the oxygen preheater 26 is adjusted by a flow control valve 27. In the oxygen preheater 26, the thermoelectric conversion element 44 is placed on the way of transferring the heat of the reacted fluid to the liquid oxygen.
As a result, a temperature gradient is generated in the thermoelectric conversion element 44, and an electromotive force is generated. In the heat released from the fluid after the reaction,
What is not converted to electric power is transmitted to the liquid oxygen 103.
A part of the fluid after passing through the preheater 2a is exhaust gas heater 1
2 and water 10 for thinning dewatered sludge.
8 used as part of

The fluid 104 separated as a gas component by the gas-liquid separator 4 blows fuel in the combustor 13 and burns.
Since oxygen is supplied in excess of the theoretical oxygen amount in the oxygen mixer 3 in order to oxidize all organic substances in the reactor 1, the fluid after the reaction contains oxygen to some extent. Therefore, combustion can be performed by injecting only the fuel in the combustor 13. Since the combustor 13 has a high pressure, liquid fuel is used as the fuel.

The fluid 104 whose temperature has risen by the combustion is sent to the high-pressure gas turbine 5, where it performs work.
The inlet pressure of the gas turbine 5 is almost the same as the critical pressure of water. If the pressure is adiabatically expanded to the atmospheric pressure at a stretch, the temperature drops too much on the way and carbon dioxide is liquefied. In order to prevent this, the fluid is once sent to the exhaust gas heater 12 during the expansion and reheated. Treated wastewater is used as the heat source of the exhaust gas heater 12. Since the outlet temperature of the gas turbine 5 is very low, heat can be extracted from the treated wastewater. The gas reheated by the exhaust gas heater 12 is sent to a low-pressure gas turbine 6 where it expands to atmospheric pressure and is generated by a generator 9 connected to the shafts of the gas turbines 5 and 6. You.

In controlling the oxygen flow rate, before the exhaust gas 104 separated by the gas-liquid separator 4 is sent to the combustor, the amount of oxygen contained in the exhaust gas 104 is measured by the oximeter 16 and this value is calculated. Oxygen flow controller 1 to reach the target value
7 controls the pump 7. The flow rate of oxygen can be changed by adjusting the rotation speed of the pump 7. Pump 7
In determining the rotation speed, the measurement result of the oxygen concentration meter 16, the history of the rotation speed of the pump 7, the target value of the oxygen concentration in the exhaust gas 104, and the processing fluid from the oxygen mixer 3 to the oxygen concentration meter 16 The time required to reach this is an input variable. The oxygen concentration in the exhaust gas 104 mainly depends on the amount of oxygen added when the fluid passes through the oxygen mixer 3, and the amount of oxygen mixed is proportional to the rotation speed of the pump 7. Therefore, by comparing the rotational speed of the pump 7 when the fluid obtained from the history of the rotational speed of the pump 7 passes through the oxygen mixer 3 and the measurement result of the oximeter 16, a correlation function between the rotational speed and the oxygen concentration is obtained. Can be requested. Oxygen flow rate control is performed so that the oxygen concentration and rotation speed data are updated as needed, and the rotation speed at which the oxygen concentration reaches the target value is obtained while constantly correcting the correlation function between the rotation speed and oxygen concentration. The device 17 controls the pump 7.

The target value of the oxygen concentration in the exhaust gas 104 is determined in advance. This is determined by the following idea. Assuming only the carbon, hydrogen, oxygen, and nitrogen components as the chemical reaction of the portion related to the exhaust gas, the following formula is obtained.

Embedded image Considering the components of the object to be treated as carbon, hydrogen, oxygen, nitrogen, etc., and expressing the mass fraction of each using X,

Embedded image The mass flow rate of the treatment target is MR, and the mass flow rate of oxygen is MO2
Then, the mass flow rate of the product is as follows.

Embedded image

Embedded image

Embedded image When the excess ratio of oxygen is λ,

Embedded image

Embedded image That is, it is sufficient to supply the oxygen amount obtained in (Chem. 7) to the set oxygen excess ratio λ. The oxygen concentration <O2> contained in the exhaust gas at this time is as follows.

Embedded image

Α in (Chemical Formula 8) represents the rate of decrease as carbon dioxide dissolves in water. The amount of carbon dioxide dissolved in water is determined by the partial pressure of carbon dioxide in the gas phase and the flow rate of water. From the above, once the composition of the raw material is determined, the target value of the oxygen concentration in the exhaust gas is determined. This means that controlling the oxygen concentration in the exhaust gas controls the oxygen excess ratio λ.

FIG. 2 shows another embodiment of the supercritical water oxidation treatment system of the present invention. This configuration differs from the configuration of FIG. 1 in that the preheater is provided in three stages, a part of the preheated fluid is returned to the downstream side of the pump 8, and the fluid 10 immediately after the reaction is used.
2 through the solid-liquid separator 18 immediately, the hydraulic drive pump 1
0 is applied to the gas-liquid separator 35, the high-temperature heat source when generating power by thermoelectric conversion is steam separated by the gas-liquid separator 35, and the heat source of the exhaust gas heater 12 is connected to the preheater 2a. That the fluid before entering is branched, and that the fluid after reaction exiting the preheater 2a is used for preheating oxygen.
Without having a combustor for heating the exhaust gas 104, measuring the oxygen concentration of the exhaust gas with the gas after passing through the gas turbine 6, adjusting the oxygen flow using the oxygen flow control valve 15, and treating the fluid to be treated. Is a mixture of low-concentration sludge 121 and waste plastic 120.

When treating the low-concentration sludge 121 that has not been concentrated, the amount of heat generated per unit mass of the processing fluid can be secured by mixing the waste plastic 120, and the autonomous operation can be performed without using an external heat source. Can be performed. Waste plastic is preheated by a crusher 22
Crush to a size about half the diameter of the inner tube of b. Since waste plastics hardly thermally decompose in the preheater 2a, the size to be crushed is based on the diameter of the inner tube of the preheater 2b having a small diameter.

The fluid 101 in which low-concentration sludge and waste plastic are mixed in the mixing tank 23 is pressurized by the pump 8 and then heated by the preheater 2a, and thereafter, is heated by the preheaters 2b and 2c.
Pass through. After the ash is removed from the fluid 102 after the reaction in the reactor 1 by the solid-liquid separator 18, the fluid 102 is sent to the preheater 2c to give heat to the fluid before the reaction, and water as the main component of the fluid is removed. It is no longer supercritical. This fluid is applied to the gas-liquid separator 4, and the fluid 105 from which gas components have been removed is sent to the preheater 2b. The fluid 105 exiting the preheater 2b is supplied to the hydraulic pump 1
The pressure is reduced at this outlet to generate a gas phase. The fluid that has become a gas-liquid two-phase is a low-pressure gas-liquid separator 35.
To separate gas and liquid. The vapor 122, which is a gaseous phase, is used as a high-temperature heat source of the thermoelectric conversion element, and the liquid phase is divided into a liquid sent to the preheater 2a and a liquid sent to the exhaust gas heater 12.

The advantage that the preheater 2b and the preheater 2c are separated is that the reacted fluid 102 can be gas-liquid separated after passing through the preheater 2c. This allows the fluid 102
The gas and liquid can be separated before the temperature of the exhaust gas drops excessively, and the exhaust gas 104 can be taken out at a high temperature. Therefore, much energy can be recovered from the exhaust gas without providing a combustor as shown in FIG. Further, since the combustor is not provided, the oxygen concentration is measured at the outlet of the gas turbine 6, and the oxygen concentration is measured at atmospheric pressure.
6 can be used. The advantage of bringing the solid-liquid separator 18 immediately after the reactor 1 is that the ash does not flow to the preheater, thereby preventing the ash from adhering to the heat transfer surface.

By performing gas-liquid separation after leaving the hydraulic drive pump 10, high-temperature steam 122 is produced, and a good high-temperature heat source for performing thermoelectric conversion is obtained. The thermoelectric conversion element 44 is placed in the oxygen preheater 26a, and performs power generation using the temperature difference between water vapor and liquid oxygen. Since the voltage generated by the thermoelectric conversion element 44 is proportional to the temperature difference between the water vapor and the liquid oxygen, the temperature of the liquid oxygen cannot be raised too much to increase this voltage. Therefore, the oxygen preheated by the oxygen preheater 26a is further preheated by the oxygen preheater 26b. At this time, the fluid after the reaction that has exited the preheater 2a is used as the heat source. Using the fluid after the reaction before entering the preheater 2a as the heat source of the exhaust gas heater 12 can increase the inlet temperature of the gas turbine 6 as compared with the configuration of FIG. Can be increased.

In controlling the oxygen amount, the use of the oxygen flow control valve 15 simplifies the control device. In calculating the valve opening of the oxygen flow control valve 15 with the oxygen flow controller 17, the measurement result of the oxygen concentration meter 16, the history of the valve opening of the oxygen flow control valve 15, the target value of the oxygen concentration, The processing fluid is supplied from the oxygen mixer 3 to the oxygen concentration meter 16.
Is the input variable. The valve opening when the fluid passes through the oxygen mixer 3 is obtained from the history of the valve opening, and the result is compared with the measurement result of the oximeter 16 to obtain a correlation function between the valve opening and the oxygen concentration. I can do it. Oxygen concentration and valve opening data are updated as needed, and the valve opening at which the oxygen concentration reaches the target value is obtained while constantly correcting the correlation function between the valve opening and oxygen concentration. The oxygen flow controller 17 controls the oxygen flow control valve 15.

FIG. 3 shows still another embodiment of the supercritical water oxidation treatment system of the present invention. 1 and 2 is that the fluid 102 after the reaction is
b, the order in which they flow into the 2c is different, a part of the fluid after the reaction is mixed with the fluid before the reaction, the air 111 is used as an organic oxidant, and the oxygen mixer 3 is connected to the preheater 2b. Beforehand, driving the hydraulic motor 11 of the positive displacement motor with the fluid 105 after the reaction, the gas-liquid separator 35
The use of the steam 122 separated in the above as a heat source of the exhaust gas heater 12, the fact that the fluid to be treated is the sludge 109 subjected to the concentration treatment, and the like. When the fluid to be treated is concentrated sludge, it can be passed directly to the oxidation treatment system.

The fluid 101 obtained by mixing a part of the fluid after the reaction with the concentrated sludge 109 is pressurized by the pump 8a, sent to the preheater 2a, and then pressurized by the pump 8b and compressed by the oxygen mixer 3. Mix air. The fluid mixed with air is sent to the reactor 1 after passing through the preheaters 2b and 2c. Reactor 1
Is first sent to the preheater 2b, then passes through the gas-liquid separator 4, the gas component is sent to the gas turbine 5, and the liquid side is sent to the solid-liquid separator 18. The fluid 105 from which the solid components have been removed by the solid-liquid separator 18 is sent to the preheater 2c. The fluid that has exited the preheater 2 c is worked by the hydraulic motor 11 and then sent to the gas-liquid separator 35. Gas-liquid separator 35
The water vapor 122 separated in the above is sent to the exhaust gas heater 12, and the liquid phase is separated into one that is sent to the preheater 2a and one that is mixed with the fluid before the reaction.

The advantage that the flow of the fluid 102 after the reaction is different from that in the embodiment of FIG. 2 is that the fluid before the reaction, which is pressurized to a high pressure, can be rapidly heated. When treating sewage sludge, the high viscosity causes a problem in passing through a preheater, but sewage sludge has a property that the viscosity is extremely reduced when heated at about 200 to 300 ° C. In order to make use of this property, the fluid having the highest temperature immediately after the reaction is placed in the preheater 2b.
The pressure loss in the preheater can be reduced by exchanging heat with the sludge and rapidly reducing the viscosity of the sludge. For the same reason, it is also effective to mix the fluid after the reaction with the fluid before the reaction to increase the temperature. Here, the flow rate to be mixed is adjusted by the flow control valve 27. In addition, by setting the position where the oxidizing agent is mixed in front of the preheater 2b, the oxidizing agent can be heated at the same time by the preheating device, so that a preheating device for the oxidizing agent becomes unnecessary. Moreover, the fact that the gas-liquid two-phase flow is used for flowing sludge into the preheater also leads to a reduction in pressure loss.

The use of air as an oxidizing agent has the advantage that running costs are lower than the use of pure oxygen. However, the power of the compressor 40 is very large as compared with the case where liquid oxygen is pressurized. In order to minimize the power required for air compression, it is effective to reduce the air flow rate to a necessary amount. As control for this, the oxygen concentration of the exhaust gas is measured as in the case of FIG. 1, and the rotation speed of the air compressor 40 is controlled. By connecting the output shaft of the hydraulic motor 11 and the rotating shaft of the pump 8b, the power required for driving the pump 8b is reduced. Water pressure motor 1
FIG. 8 shows a reciprocating axial piston motor as one example. The piston is driven by the high-pressure fluid 125,
The shaft 45 rotated thereby becomes the output shaft.

FIG. 4 shows still another embodiment of the supercritical water oxidation treatment system of the present invention. This configuration is different from the configurations of FIGS. 1 to 3 in that the hydraulic drive pump 10 is used as a low-pressure pump, a heat exchanger 19 for heating the exhaust gas with a fluid immediately after the reaction is provided, and a peroxide is used as an oxidizing agent. For example, the hydrogen water 110 is used. The hydrogen peroxide solution 110 is supplied through the pump 33 and preheated by the heat exchanger 46, and then the flow rate is adjusted by the flow control valve 34 and mixed with the concentrated sludge 109. The fluid 101 mixed with the hydrogen peroxide solution is pressurized by the hydraulic drive pump 10 and sent to the preheater 2a. Thereafter, the fluid pressurized by the pump 8 is supplied to the preheater 2
It is heated in b and sent to the reactor 1. Fluid after reaction 10
2 is sent to a heat exchanger 19 for heating the exhaust gas, and after giving heat to the exhaust gas, is sent to a preheater 2b. The fluid that has exited the preheater 2b passes through the gas-liquid separator 4 and the solid-liquid separator 18, and the liquid phase component is sent to the preheater 2a. The gas component is the heat exchanger 1
9, heated by the high-temperature fluid 102 immediately after the reaction, and sent to the turbine 5. Fluid 10 exiting preheater 2a
Numeral 5 is sent to the hydraulic drive pump 10 and serves to drive the pump.

By using the fluid immediately after the reaction for heating the exhaust gas, the exhaust gas can be heated by using the highest temperature when no external heat source is used, and even when only one gas turbine is operated. Energy can be sufficiently recovered. The advantages of using hydrogen peroxide as an oxidizing agent are that it is cheaper than pure oxygen, and because hydrogen peroxide is liquid, it requires less compressor power than when air is compressed. and so on.

FIG. 5 shows still another embodiment of the supercritical water oxidation treatment system of the present invention. This configuration is different from the configurations of FIGS. 1 to 4 in that oxygen is extracted from the fluid after the reaction, and the oxygen is reused. The hydraulic motor 11 is driven by the fluid after the reaction to generate power; The vessel is divided into two stages, and both the fluid 105 before entering the preheater 2a and the fluid leaving the hydraulic motor 11 are used as heat sources for the oxygen preheater. The carbon dioxide 112 is removed from the exhaust gas 104 separated by the gas-liquid separator 4 by the carbon dioxide separator 20, and then the liquid oxygen 113 is extracted by the oxygen separator 21. The extracted liquid oxygen 113 is used by mixing with the supplied liquid oxygen 103.

FIG. 9 shows an example of the configuration of the carbon dioxide separator 20. The supercritical exhaust gas 104 containing carbon dioxide, oxygen, and nitrogen as main components is sent to the expansion turbine 5, where it performs adiabatic expansion to power the generator 50. Since the water vapor contained therein is liquefied with the temperature decrease of the fluid due to the adiabatic expansion, the water vapor is separated by the water drop separator 38,
The water 108 is removed. The fluid from which water has been removed is cooled by passing through the heat exchangers 30a, 30b, 30c, and only carbon dioxide having a high boiling point is condensed and liquefied. A gas mixture of liquid carbon dioxide and other gases is separated into a gas phase and a liquid phase by a gas-liquid separator 29. Gas-liquid separator 29
The main components of the gas 117 separated in the above are oxygen and nitrogen. Liquid carbon dioxide 119 separated by gas-liquid separator 29
The pressure is reduced by passing through the expansion valve 32c, and the temperature is reduced by partially vaporizing. The carbon dioxide gas-liquid two-phase passed through the expansion valve 32c passes through the heat exchanger 30c and removes heat from the fluid before the carbon dioxide is separated.
The carbon dioxide whose dryness has increased in the heat exchanger 30c is supplied to the expansion valve 3
By passing through 2b, the pressure is reduced, and the gas phase increases and the temperature decreases at the same time. The gas-liquid two-phase carbon dioxide that has passed through the expansion valve 32b passes through the heat exchanger 30b and removes heat from the fluid before the carbon dioxide is separated. Most of the carbon dioxide is vaporized at the outlet of the heat exchanger 30b and sent to the expansion valve 32a. By passing through the expansion valve 32a, the carbon dioxide that has become atmospheric pressure passes through the heat exchanger 30a, and removes heat from the fluid before the carbon dioxide is separated. Used in

FIG. 10 shows an example of the configuration of the oxygen separator 21. The gas 117 containing oxygen and nitrogen as main components is compressed by the compressor 37 and then cooled by passing through the heat exchanger 30d. At this time, a mixed fluid of carbon dioxide 112 generated by the carbon dioxide separator and gas 114 mainly containing nitrogen is used as the cold heat source. The fluid that has exited the heat exchanger 30d is adiabatically expanded by the expansion turbine 5 to lower the temperature. Since the carbon dioxide 127 contained in the fluid 117 is liquefied due to the decrease in the temperature, the carbon dioxide 127 is removed by the gas-liquid separator 48. The fluid from which carbon dioxide has been removed is further cooled in the heat exchanger 30e, and then decompressed by passing through the expansion valve 32d. When the pressure is reduced by the expansion valve 32d, oxygen having a boiling point higher than that of nitrogen is liquefied at the same time as the temperature is lowered. The fluid that has become a gas-liquid two phase is separated into a gas phase and a liquid phase by a gas-liquid separator 31, and the liquid phase is taken out as liquid oxygen 113 and used. The gas 114 containing nitrogen as a main component separated by the gas-liquid separator 31 is decompressed by the expansion valve 32e and becomes atmospheric pressure. Fluid 1 whose temperature has decreased due to expansion at this time
By passing 14 through heat exchanger 30e, heat is removed from the fluid before oxygen is separated.

Returning to FIG. 5, the oxygen preheater 26b uses a fluid obtained by branching the reacted fluid 105 into a heat source, and further preheats the oxygen once preheated by the oxygen preheater 26a. In the oxygen preheater 26a, the fluid exiting the oxygen preheater 26b and the fluid exiting the hydraulic motor 11 are mixed and used as a heat source.
Since the oxygen preheater is divided into two stages of 26a and 26b, oxygen can be preheated to a temperature close to the temperature of the fluid 105.

FIG. 6 shows still another embodiment of the supercritical water oxidation treatment system of the present invention. This configuration is different from the configurations of FIGS. 1 to 5 in that an absorption refrigerator 28 is provided, and the exhaust gas 104 is used as a heat source of the oxygen preheater 26, and thereafter, the fluid 115 is provided to the outside as a cold heat source. In performing power recovery from the fluid 105 after the reaction,
For example, a positive displacement rotary hydraulic motor 41 is used.
After the reaction, the fluid 102 passes through the preheater 2b and drops in temperature. Then, the gas component is separated by the gas-liquid separator 4, and the liquid phase is passed through the solid-liquid separator 18 to remove the solid component 106. The fluid 105 from which the solid components have been removed is worked by the hydraulic motor 41, then passes through the gas-liquid separator 35 and is sent to the preheater 2a. The water vapor 122 separated by the gas-liquid separator 35 is sent to the absorption refrigerator 28 and used as a high-temperature heat source of the absorption refrigerator. Cold water 116 produced by the absorption refrigerator is provided outside and used as a cold heat source.

The exhaust gas 104 separated by the gas-liquid separator 4 is sent to the oxygen preheater 26, where it is used as a high-temperature heat source for the thermoelectric conversion element and, at the same time, preheats oxygen. As a result, the exhaust gas 104 whose temperature has decreased is reduced in pressure by passing through the expansion valve 32, and the temperature further decreases. This low-temperature fluid 115 is provided outside and is used as a cold heat source. The fluid 105 after the reaction is driven by the rotary hydraulic motor 41 to generate power by the generator 9 connected thereto. Rotary hydraulic motors include gear motors and screw motors. By using a rotary hydraulic motor,
The fluid 105 flows smoothly without pulsation.

[0055]

As described above, according to the present invention, the exhaust gas and waste water generated by the oxidation treatment of organic substances with supercritical water are separated into a gaseous phase and a liquid phase, and energy is separately recovered.
The effective energy of the fluid after the oxidation treatment can be fully utilized, and the energy efficiency of the entire system is improved. Also, by utilizing the fact that the exhaust gas is generated under high pressure, oxygen contained in the exhaust gas is separated and extracted and reused, thereby reducing oxygen consumption and reducing running costs. In addition, the overall energy efficiency is improved by driving the absorption refrigerator using the heat energy of the wastewater or by generating cold heat by expanding high-pressure exhaust gas and providing it to the outside. In addition, by using the temperature difference between exhaust gas or wastewater and liquid oxygen to generate power using a thermoelectric conversion element, electric power can be obtained, and at the same time heat not converted to electric power is used for preheating liquid oxygen. , Increase the energy recovery rate. Further, by crushing the solid organic matter into a size suitable for the heat transfer tube of the preheater, the heat transfer coefficient of the fluid can be improved, and the preheater can be downsized.
Further, by controlling the flow rate of the supplied oxygen by measuring the oxygen concentration of the exhaust gas, it is possible to suppress the consumption of oxygen and reduce the running cost while maintaining a favorable oxidation reaction.

[Brief description of the drawings]

FIG. 1 is a first diagram of a supercritical water oxidation treatment system according to the present invention.
FIG. 2 is a system diagram showing a configuration example of FIG.

FIG. 2 shows a second embodiment of the supercritical water oxidation treatment system according to the present invention.
FIG. 2 is a system diagram showing a configuration example of FIG.

FIG. 3 shows a third embodiment of the supercritical water oxidation treatment system according to the present invention.
FIG. 2 is a system diagram showing a configuration example of FIG.

FIG. 4 is a fourth diagram of the supercritical water oxidation treatment system according to the present invention.
FIG. 2 is a system diagram showing a configuration example of FIG.

FIG. 5 is a fifth diagram of the supercritical water oxidation treatment system according to the present invention.
FIG. 2 is a system diagram showing a configuration example of FIG.

FIG. 6 shows a sixth embodiment of the supercritical water oxidation treatment system according to the present invention.
FIG. 2 is a system diagram showing a configuration example of FIG.

FIG. 7 is a diagram showing a configuration of a hydraulic drive pump to which pistons having different cross-sectional areas are connected.

FIG. 8 is a diagram showing a configuration of a reciprocating hydraulic motor.

9 is a diagram showing a configuration of a carbon dioxide separation device suitable for the system of FIG.

FIG. 10 is a diagram showing a configuration of an oxygen separation device suitable for the system of FIG.

FIG. 11 is a schematic diagram when a fluid mixed with dewatered sludge flows through a preheater.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Reactor 2 Preheater 3 Oxygen mixer 4 Gas-liquid separator 5, 6 Gas turbine 7 Liquid oxygen pump 8 Pump 9, 50 Generator 10 Hydraulic drive pump 11 Water pressure motor 12 Exhaust gas heater 13 Combustor 14 a, 14 b Electromagnetic Induction heater 16 Oxygen concentration meter 17 Oxygen flow controller 18 Solid-liquid separator 20 Carbon dioxide separator 21 Oxygen separator 22 Crusher 26 Oxygen preheater 28 Absorption refrigerator 32 Expansion valve 44 Thermoelectric conversion element 101 Reaction containing organic matter Fluid before 102 Fluid after reaction 104 Exhaust gas separated by gas-liquid separator 105 Wastewater separated by gas-liquid separator 106 Ash separated by solid-liquid separator 107 Dehydrated sludge 108 Water 109 Concentrated sludge 110 Hydrogen peroxide Water 111 air

 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Hiroshi Kusumoto 502, Kandachi-cho, Tsuchiura-shi, Ibaraki Machinery Research Laboratory, Hitachi, Ltd. (72) Inventor Shinji Aso 1-13-1-2 Kita-Otsuka, Toshima-ku, Tokyo Hitachi Within Plant Construction Co., Ltd. (72) Inventor Hitoshi Kawajiri 1-13-2 Kita-Otsuka, Toshima-ku, Tokyo Hitachi Plant Construction Co., Ltd. (72) Inventor Tetsuji Miyabayashi 537 Kamigo, Matsudo-shi, Chiba Hitachi Plant Construction Co., Ltd. Inside Matsudo Research Laboratory (72) Inventor Ryuichi Kaji 4-6 Kanda Surugadai, Chiyoda-ku, Tokyo Inside Hitachi, Ltd. (72) Inventor Takao Sato 3-1-1 Komachi, Hitachi, Hitachi, Ibaraki Hitachi, Ltd. in the factory

Claims (14)

[Claims] 1. A method of oxidizing a fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction close to the supercritical state to promote the reaction; and gas-liquid separation for separating the fluid after the reaction into a gas component and water. And a gas power generation means for recovering power using the gas components separated by the gas-liquid separation means. A supercritical water oxidation treatment system for organic matter, comprising: 2. A gas component heating means for heating the gas component used in the gas power generation means by using thermal energy of the reacted fluid separated as water by the gas-liquid separation means. The supercritical water oxidation treatment system for organic matter according to claim 1. 3. A method of oxidizing a fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction close to the supercritical state to promote the reaction; and gas-liquid separation for separating the fluid after the reaction into a gas component and water. Means for driving a piston with the fluid after reaction separated as water by the gas-liquid separation means, pressurizing the fluid before reaction with a piston interlocking with the piston, and a cross section of the piston in contact with the fluid before reaction. Water-driven pressurizing means configured to have a smaller area than a cross-sectional area of a piston in contact with the fluid after the reaction, and a system for supercritical water oxidation of organic matter. 4. A method of oxidizing a fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction close to the supercritical state to promote the reaction; and gas-liquid separation for separating the fluid after the reaction into a gas component and water. Means, carbon dioxide separation means for separating carbon dioxide from the gas component separated by the gas-liquid separation means, and oxygen separated from the gas component from which carbon dioxide has been removed by the carbon dioxide separation means. Supercritical water treatment system of organic matter, characterized by comprising an oxygen separation and recovery means for mixing the fluid before reaction, the. 5. A method of oxidizing a fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction close to the supercritical state to promote the reaction; and gas-liquid separation for separating the fluid after the reaction into a gas component and water. And an absorption refrigeration unit that operates using the gas component separated by the gas-liquid separation unit as a heat source. 6. A fluid containing an organic substance and oxygen or an oxidant in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. Preheating means for removing water in the fluid from the supercritical state, and bringing water in the fluid before the reaction close to the supercritical state to promote the reaction, and generating electric power by using thermal energy of the fluid after the reaction as a driving source A supercritical water oxidation treatment system for organic matter, comprising: thermoelectric conversion means. 7. A fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recover energy from the fluid after the oxidation reaction has been performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction close to the supercritical state to promote the reaction; and gas-liquid separation for separating the fluid after the reaction into a gas component and water. And a positive displacement hydraulic motor that recovers power by being driven by the fluid after the reaction separated as water by the gas-liquid separation means. . 8. A fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction closer to the supercritical state to promote the reaction; and a part of the fluid before the reaction heated by the preheating means, A reflux means for mixing with a fluid before being heated by the preheating means; and a supercritical water oxidation treatment system for organic matter. 9. A method of oxidizing a fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. A preheating means for removing water in the fluid from the supercritical state and bringing the water in the fluid before the reaction close to the supercritical state to promote the reaction; and gas-liquid separation for separating the fluid after the reaction into a gas component and water. And a cooling means for generating a temperature lower than that of the outside air by rapidly expanding the gas component separated by the gas-liquid separation means. 10. A fluid containing an organic substance and oxygen or an oxidant in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. In a supercritical water oxidation treatment system for organic substances, the post-reaction fluid is supplied to the pre-reaction fluid by flowing the post-reaction fluid to the outside of a heat transfer tube through which the pre-reaction fluid containing organic substances flows. Preheating means to remove water in the fluid from supercritical state and bring water in the fluid before the reaction closer to supercritical state to promote the reaction, and heat water in the fluid before the reaction using electromagnetic induction heating A supercritical water oxidation treatment system for organic matter, comprising: heating means. 11. The apparatus according to claim 1, further comprising a plurality of stages each of said preheating means and a pressurizing means for pressurizing a fluid before reaction flowing into said preheating means.
A supercritical water oxidation treatment system for organic matter according to any one of the above. 12. An oxygen or oxidizing agent heating means for heating oxygen or oxidizing agent to be added to a pre-reaction fluid containing an organic substance using water as a solvent by the thermal energy of the post-reaction fluid. Claim 1 to Claim 1
0. A supercritical water oxidation treatment system for organic matter according to any one of the above. 13. The apparatus according to claim 1, further comprising a granulating means for granulating organic matter to a size of not more than half the diameter of the heat transfer tube of the preheater. The supercritical water oxidation treatment system for organic matter according to the above. 14. A fluid containing an organic substance and oxygen or an oxidizing agent in a supercritical state using water as a solvent to oxidize the organic substance, and recovering energy from the fluid after the oxidation reaction is performed. An operation method of an organic matter supercritical water oxidation treatment system, comprising: oxygen concentration measuring means for measuring an oxygen concentration in a gas component of a reacted fluid after water in the fluid after the reaction is no longer in a supercritical state; And oxygen or oxidizing agent control means for controlling the amount of oxygen or oxidizing agent to be mixed with the fluid containing organic matter, wherein the oxygen concentration in the gas component of the reacted fluid measured by the oxygen concentration measuring means is predetermined. A step of controlling the amount of oxygen or oxidizing agent to be mixed so that the oxygen or oxidizing agent is controlled so as to reach a target value. The stem method of operation.