JP4306028B2 - Organic substance oxidation treatment system and oxidation treatment method - Google Patents

Description

【００３９】
（数１）において、γは水の比熱比で、有機物の酸化処理に用いられる高温高圧水では１．５乃至１．６の値である。
【００４０】
図５は、（数１）の関係を横軸にＰ／Ｐ０、縦軸にＡ／Ａ＊として示したグラフである。図５に示すように、絞り機構４１を用いて処理流体を減圧させるということは、Ｐ／Ｐ０が１より小さいということなので、いずれの圧力比においても流路断面積比Ａ／Ａ＊は１より大きくなければならない。
【００４１】
すなわち、絞り機構は、絞り機構出口における流路断面積が、最も流路断面積が小さい部分の流路断面積よりも大きいような形状である必要がある。
【００４２】
絞り機構４１の流路断面を末広がりの形状とすることにより、圧縮性流体の性質として、絞り機構４１の出口の流体温度は絞り機構４１の入口の流体温度に比べて自動的に低くなる。従って、背圧器５０に流通される流体の温度は、反応器４０内部の流体の温度に比べて低くなる。
【００４３】
尚、図１、または図２に示す第１の実施の形態例では、絞り機構４１は流路断面形状が円形の場合を示しているが、流路断面形状は処理流体が流通するものであれば任意の形状でよい。
【００４４】
反応器内の酸化反応が、例えば水の超臨界状態で行われる場合、反応後の流体は温度が約３８０℃、圧力が約２２ＭＰａとなる。背圧器を設けずに、且つ、弁等を用いて減圧の度合いを調節しようとすると、弁の可動部が高温高圧の流体に曝されることになり、可動部の材料強度等の問題から、弁の信頼性が低くなり、ひいては処理システム全体の信頼性低下に繋がる。
【００４５】
図１に示す第１の実施の形態例によれば、絞り機構４１を末広がりノズルで構成し、絞り機構４１に背圧器５０を設け、さらに、気液分離器７０からの気相部分を弁５２を介して背圧器５０に導入する構成とすることにより、減圧の度合い、すなわち、背圧器５０の圧力を弁５２で調整できる。
【００４６】
気液分離７０から供給される気相の温度は、予熱器３０を通過するため、反応直後の流体の温度よりは低く、弁５２の信頼性を高めることでき、且つ、調整が容易となる。また、絞り機構４１が可動部を持たないため、高温高圧の条件でも安定して機能することができ、結果として、システム全体の信頼性を高めることができる。
【００４７】
また、背圧器５０内の圧力は、絞り機構４１により減圧されるため、反応器４０よりも低い圧力に耐えられるものであればよい。
【００４８】
尚、図１において、酸素の代わりに空気等の他の酸化剤を用いてもよい。
【００４９】
図６は、本発明の第２の実施の形態例に係わる有機物の酸化処理システムを示す系統図である。この構成で図１と異なっているのは、反応器が反応器４０Ａと反応器４０Ｂとで構成され、反応器４０Ａと４０Ｂはシリーズに接続されて設けられ、前記反応器４０Ａ内の流体は、一部は絞り機構４１Ａを通して背圧器５０に導入され、残りの部分は反応器４０Ｂに導入され、反応器４０Ｂ内の流体は、一部は絞り機構４１Ｂを通して背圧器５０に導入され、残りの部分は予熱器３０に導入されている点で、それ以外は図１に示す実施の形態例と同じである。
【００５０】
図６に示す第２の実施の形態例によれば、前段の反応器４０Ａに設けられた絞り機構４１Ａで排出されない固形物がある場合でも、後段の反応器４０Ｂに設けられた絞り機構４１Ｂにより固形物を排出することが可能である。
【００５１】
このように、絞り機構を備えた反応器をシリーズに接続することにより、固形物の除去効率を高めることができる。
【００５２】
尚、図６に示す実施の形態例では、２つの反応器にそれぞれ設けられた絞り機構が１つの背圧器に連通されているが、各々の反応器に個別の背圧器を設けてもよい。
【００５３】
また、図６に示す実施の形態例では、２つの反応器がシリーズに接続されている場合を示したが、３つ以上の反応器をシリーズに接続することにより、さらに良好な固形物分離を行うことができる。
【００５４】
図７は、本発明の第３の実施の形態例に係わる有機物の酸化処理システムを示す系統図である。図７に示す第３の実施の形態例の処理システムは、有機物用タンク１０と、有機物供給ポンプ１１と、酸素用タンク２０と、酸素供給ポンプ２１と、酸素供給用弁２２と、予熱器３０と、反応器４０Ａ,４０Ｂと、絞り機構４１Ａ,４１Ｂと、弁４２Ａ,４２Ｂと、弁４３Ａ,４３Ｂと、背圧器５０Ａ,５０Ｂと、集塵器６０と、背圧器及び集塵器を連通する弁５１Ａ,５１Ｂと、気液分離器７０と、気液分離器及び背圧器を連通する弁５２Ａ,５２Ｂとから構成されている。
【００５５】
有機物用タンク１０内に貯えられた含水有機物１０Ａは、有機物供給ポンプ１１により予熱器３０に導入される。一方、酸素用タンク２０に貯えられた酸素２０Ａは、酸素供給ポンプ２１により供給され、予熱器３０により予熱された有機物と混合される。酸素２０Ａと混合後の有機物は、反応器４０Ａを含む系統および／または反応器４０Ｂを含む系統に導入される。
【００５６】
反応器４０Ａを含む系統では、弁４２Ａ,４３Ａ及び弁５１Ａ,弁５２Ａが開いている場合、酸素２０Ａと混合された有機物は、反応器４０Ａに導入され、高温高圧下で酸化反応される。
【００５７】
反応後の流体は、一部は絞り機構４１Ａを通して背圧器５０Ａに導入され、残りの部分は弁４３Ａを介して予熱器３０に導入される。予熱器３０に導入され、反応前の有機物と熱交換した前記反応後の流体は、気液分離器７０に導入され、気相と液相に分離された後、気相の部分が弁５２Ａを介して前記背圧器５０Ａに導入される。
【００５８】
背圧器５０Ａでは、絞り機構４１Ａを通して背圧器に導入される反応後の流体が、気液分離器７０より発生した気相と概略同等の圧力まで減圧される。減圧されることにより、反応処理後の流体の水分の沸点が下がり、水分は蒸発し、前記反応後の流体は水蒸気と固形物に分離される。
【００５９】
分離された水蒸気と固形物は、背圧器５０Ａと弁５１Ａを介して連通された集塵器６０に導入され、固形分は集塵器６０により捕捉され、除去される。
【００６０】
反応器４０Ｂを含む系統では、弁４２Ｂ,４３Ｂ及び弁５１Ｂ,弁５２Ｂが開いている場合、酸素２０Ａと混合された有機物は、反応器４０Ｂに導入され、高温高圧下で酸化反応される。
【００６１】
反応後の流体は、一部は絞り機構４１Ｂを通して背圧器５０Ｂに導入され、残りの部分は弁４３Ｂを介して予熱器３０に導入される。予熱器３０に導入され、反応前の有機物と熱交換した前記反応後の流体は、気液分離器７０に導入され、気相と液相に分離された後、気相の部分が弁５２Ｂを介して背圧器５０Ｂに導入される。
【００６２】
背圧器５０Ｂでは、絞り機構４１Ｂを通して背圧器に導入される反応後の流体が、気液分離器７０より発生した気相と概略同等の圧力まで減圧される。減圧されることにより、反応処理後の流体の水分の沸点が下がり、水分は蒸発し、前記反応後の流体は水蒸気と固形物に分離される。
【００６３】
分離された水蒸気と固形物は、背圧器５０Ｂと弁５１Ｂを介して連通された集塵器６０に導入され、固形分は集塵器６０により捕捉され、除去される。
【００６４】
図７に示す第３の実施の形態例によれば、反応器４０Ａを含む系統と、反応器４０Ｂを含む系統とを共に稼動させることにより、有機物の処理量を多くすることが可能となる。
【００６５】
また、反応器４０Ａを含む系統と、反応器４０Ｂを含む系統のどちらか一方の系統で、反応を停止させて部品交換等の保守、点検作業が必要な場合、他方の系統を稼動させることにより、保守、点検作業時においてもシステム全体を停止させることなく処理を行うことができ、システムの信頼性を高めることができる。
【００６６】
尚、図７に示す実施の形態例では、反応器を含む系統が２つ並列に設けられている場合を示したが、反応器を含む系統を３つ以上並列に接続することにより、さらに信頼性の高いシステムを構成することができる。
【００６７】
図８は、本発明の第４の実施の形態例に係わる有機物の酸化処理システムを示す系統図である。この構成で図７と異なっているのは、集塵器が集塵器６０Ａと集塵器６０Ｂとで構成され、集塵器６０Ａは弁５１Ａを介して背圧器５０Ａと連通して設けられ、集塵器６０Ｂは弁５１Ｂを介して背圧器５０Ｂと連通して設けられている点で、それ以外は図７に示す実施の形態例と同じである。
【００６８】
図８に示す第４の実施の形態例によれば、集塵器６０Ａまたは６０Ｂの一方において、集塵能力の低下等により保守、点検作業が必要な場合でも、他方の集塵器を含む系統を稼動させることにより、システム全体を停止させることなく、有機物の処理と、保守、点検作業を同時に行うことができるため、信頼性の高いシステムを構成することができる。
【００６９】
図９は、本発明の第５の実施の形態例に係わる有機物の酸化処理システムを示す系統図である。この構成で図１に示す第１の実施の形態例と異なっているのは、集塵器６０で固形物を除去されたあとの水蒸気Ｄを酸素予熱器８０に導入し、水蒸気Ｄと酸素２０Ａを熱交換させて、酸素２０Ａを予熱するという点で、それ以外は図１に示す実施の形態例と同じである。
【００７０】
高温水を用いた有機物の酸化処理では、反応器内で良好な酸化反応を行うためには、有機物を反応器に導入する前にある程度の温度まで予熱する必要がある。
【００７１】
図９に示す第５の実施の形態例によれば、酸素２０Ａを、酸素予熱器８０にて、集塵器から供給される水蒸気と熱交換させて予熱することにより、酸素２０Ａと有機物との混合による温度の低下を防ぐことができ、良好な酸化反応を行わせることが可能となる。
【００７２】
また、本実施の形態例によれば、酸素２０Ａを予熱するために、外部からエネルギーを投入する必要がないため、自立運転型のエネルギー利用効率の高いシステムを構成することが可能である。
【００７３】
【発明の効果】
本発明によれば、高温水を用いた有機物の酸化処理システムにおいて、反応器に絞り機構を設け、さらに、背圧器を設けたことで、固形物を含む反応処理水を連続的に反応器から排出し、且つ、連続的に固形物を除去することができる。これにより、酸化処理システムを効率的に運転させることができる。
【００７４】
また、固形物を含む反応処理水を反応器から排出する絞り機構は、可動部を持たないため、高温高圧下でも安定して機能するため、処理システム全体の信頼性を向上させることができる。
【図面の簡単な説明】
【図１】本発明の第１の実施の形態例に係わる酸化処理システムを示す系統図である。
【図２】図１の反応器の形態例を示す断面図である。
【図３】図１の反応器の形態例を示す上面図である。
【図４】図１の絞り機構の形状を示す概略図である。
【図５】絞り機構の流路断面積条件を示すグラフである。
【図６】本発明の第２の実施の形態例に係わる酸化処理システムを示す系統図である。
【図７】本発明の第３の実施の形態例に係わる酸化処理システムを示す系統図である。
【図８】本発明の第４の実施の形態例に係わる酸化処理システムを示す系統図である。
【図９】本発明の第５の実施の形態例に係わる酸化処理システムを示す系統図である。
【符号の説明】
１０…有機物用タンク、１０Ａ…含水有機物、１１…有機物供給ポンプ、２０…酸素用タンク、２０Ａ…酸素、２１…酸素供給ポンプ、３０…予熱器、４０,４０Ａ,４０Ｂ…反応器、４１,４１Ａ,４１Ｂ…絞り機構、５０,５０Ａ,５０Ｂ…背圧器、６０,６０Ａ,６０Ｂ…集塵器、７０…気液分離器、８０…酸素予熱器。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a processing system and a processing method suitable for oxidizing organic substances in a fluid under high temperature and high pressure using water as a solvent.
[0002]
[Prior art]
As for purification treatment of domestic wastewater, factory wastewater and the like containing organic substances, a method utilizing a decomposition reaction by microorganisms is widely performed. In this method, a large amount of sludge is generated during the treatment. The generated sludge is incinerated or landfilled. However, it is difficult to secure a landfill site by the method of reclaiming sludge as it is, and many of them are incinerated.
[0003]
For incineration of sludge, the method using an incinerator is the most widespread as in general incineration, but in order to make the sludge flammable, the proportion of incombustibles such as inorganic content and moisture in the sludge is reduced, or Measures such as adding fuel are necessary to support the combustion of sludge.
[0004]
Since the amount of water in sewage sludge reaches 97-98% by mass, the sludge is concentrated and dehydrated, and the water content is reduced to about 80% before being supplied to the incinerator. .
[0005]
As an alternative method, a method called a wet oxidation method has been proposed. In this method, air or oxygen is forcibly sent as an oxidizing agent under a hot water condition of about 200 to 300 ° C. and about 100 atm to cause an oxidative decomposition reaction.
[0006]
Compared with the method using an incinerator, this method has the advantage that the pretreatment can be simplified such that the amount of water in the sludge can be reduced because the sludge can be oxidized in the presence of water. Furthermore, generation of harmful gases as seen in general incinerators can be suppressed, and an exhaust gas treatment device is not required.
[0007]
However, in this method, removal of ash generated during the oxidative decomposition reaction and residual solid matter that is an unreacted material is a major problem in the construction of an oxidation treatment system.
[0008]
If solids cannot be sufficiently removed from the fluid after the decomposition reaction, there is a possibility that the pipeline for conveying the processed fluid may be blocked, leading to a decrease in the reliability of the processing system.
[0009]
In addition, as described in, for example, JP-B-1-38532, in a system that recovers and uses the thermal energy of a processing fluid using a preheater or the like, in order to distribute the processed fluid to the heat exchanger, If the solids in the treated fluid are not removed, the solids adhere to the heat transfer surface of the heat exchanger, which reduces the heat transfer performance of the heat exchanger, and the heat energy of the treated fluid. May not be used effectively.
[0010]
As a solid removal method in the oxidation treatment method using water as a medium, for example, there are a method described in JP-A-1-258800 and a method described in JP-A-8-38853. However, in the method described in the above publication, it is difficult to increase the reliability of the processing system, or heat energy is supplied from the outside when separating solids from the fluid after oxidation treatment. There is a problem that a large amount of energy is required.
[0011]
[Problems to be solved by the invention]
The object of the present invention is to provide an organic oxidation system and an oxidation treatment method that can efficiently remove solids such as incombustibles from the fluid after the oxidation reaction.
[0012]
[Means for Solving the Problems]
In order to achieve the above object, the organic oxidation system according to the present invention is characterized in that a fluid containing an organic substance and oxygen or an oxidant is subjected to an oxidation reaction under high temperature and high pressure in a reactor using water as a solvent. The processing fluid that has undergone the oxidation reaction is discharged to a back pressure device through a throttling mechanism, and the discharged processing fluid is reduced to a pressure approximately equal to that of the supplied gas to evaporate water and separate it into water vapor and solid matter.
[0013]
Specifically, the present invention provides the following systems and methods.
[0014]
The present invention relates to an organic matter oxidation treatment system that oxidizes organic matter in a fluid under high temperature and high pressure using water as a solvent, and a reaction in which the fluid containing the organic matter and oxygen or an oxidizing agent is subjected to an oxidation reaction under the high temperature and high pressure. And a throttling mechanism that is provided in the reactor and discharges the oxidized processing fluid, and evaporates water by reducing the discharged processing fluid to a pressure approximately equal to the gas supplied from the gas supply device. And a back pressure device that separates into water vapor and solid matter.
[0015]
Preferably, a dust collector for removing the separated solid matter is provided in communication with the back pressure device.
[0016]
Preferably, the gas supply device includes a gas-liquid separator that separates the processing fluid into a gas phase and a liquid phase, or an air compressor.
[0017]
Preferably, the throttle mechanism is constituted by a divergent nozzle.
[0018]
Preferably, a preheater is provided that heats the oxygen or oxidant by exchanging heat with water vapor generated by the back pressure device.
[0019]
Further, the present invention provides an organic matter oxidation treatment method in which an organic matter is oxidized in a fluid under high temperature and high pressure using water as a solvent, and the fluid containing the organic matter and oxygen or an oxidizing agent is subjected to an oxidation reaction under high temperature and high pressure. The oxidized processing fluid is discharged, and the discharged processing fluid is depressurized to a pressure lower than the gas in the processing container to evaporate water to separate it into water vapor and solids. Provided is a method for oxidizing an organic substance characterized by being captured and removed.
[0020]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, an organic oxidation system according to an embodiment of the present invention will be described with reference to the drawings.
[0021]
FIG. 1 is a system diagram showing an organic oxidation system according to a first embodiment of the present invention. The oxidation treatment system of the first embodiment includes an organic substance tank 10, an organic substance supply pump 11, an oxygen tank 20, an oxygen supply pump 21, an oxygen supply valve 22, a preheater 30, and a reactor 40. A throttle mechanism 41, a back pressure device 50, a dust collector 60, a valve 51 communicating the back pressure device 50 and the dust collector 60, a gas-liquid separator 70, a gas-liquid separator 70, and the back pressure device 50. It is comprised from the valve 52 which connects.
[0022]
The water-containing organic substance 10 </ b> A stored in the organic substance tank 10 is introduced into the preheater 30 by the organic substance supply pump 11. On the other hand, the oxygen 20 </ b> A stored in the oxygen tank 20 is supplied by the oxygen supply pump 21 and mixed with the organic matter preheated by the preheater 30.
[0023]
The water-containing organic substance mixed with the oxygen 20A is introduced into the reactor 40 and subjected to an oxidation reaction under high temperature and high pressure. A part of the fluid after the reaction is introduced into the back pressure unit 50 through the throttle mechanism 41, and the remaining part is introduced into the preheater 30.
[0024]
The fluid after the reaction introduced into the preheater 30 and heat-exchanged with the organic matter before the reaction is introduced into the gas-liquid separator 70 and separated into the gas phase and the liquid phase, and then the gas phase portion is passed through the valve 52. Is introduced into the back pressure device 50.
[0025]
In the back pressure device 50, the reacted fluid introduced into the back pressure device 50 through the throttle mechanism 41 is decompressed to a pressure approximately equal to the gas phase generated from the gas-liquid separator 70. By reducing the pressure, the boiling point of water in the fluid after the reaction treatment is lowered, the water is evaporated, and the fluid after the reaction is separated into water vapor and solid matter.
[0026]
The separated water vapor and solid matter are introduced into a dust collector 60 communicated with the back pressure device 50 and the valve 51, and the solid content is captured and removed by the dust collector 60.
[0027]
FIG. 2 is a cross-sectional view showing an example of the form of a reactor 40 for favorably operating the oxidation processing system of the first embodiment shown in FIG. FIG. 3 is a top view showing an example of the form of the reactor 40 shown in FIG.
[0028]
The reactor 40 shown in FIG. 2 or FIG. 3 has a cylindrical structure, and a throttling mechanism 41 is provided at the bottom of the reactor 40, and an organic substance is disposed on the side of the reactor 40 approximately above the reactor 40. Is provided, and a pipe 46 for discharging organic substances is provided substantially below the reactor 40, and a member 48 for forming a double flow path is provided at the bottom of the reactor 40. It has been.
[0029]
The tube 45 is provided so that the center line of the tube 45 and the center line of the reactor 40 do not intersect.
[0030]
By configuring the reactor 40 as shown in FIG. 2 or FIG. 3, the organic matter supplied from the tube 45 flows along the inner surface of the reactor 40.
[0031]
Further, since the pipe 46 for discharging the organic matter from the reactor 40 is provided substantially below the reactor, the organic matter flows from the top to the bottom while swirling inside the reactor 40, that is, in a spiral shape. A flow will be formed. At this time, the solid matter having a specific gravity heavier than water is subjected to a force in a direction away from the center of the reactor 40 due to the action of centrifugal force in the spiral flow.
[0032]
Therefore, a portion having a high solid concentration is formed in the vicinity of the inner surface of the reactor 40 and settles along the inner surface of the reactor 40 by the action of gravity. Then, the fluid having a high solid concentration that settles along the inner surface of the reactor 40 flows through the flow path between the member 48 and the reactor 40.
[0033]
Therefore, the fluid having a high solid concentration flowing through the flow path between the member 48 and the reactor 40 is not affected by the spiral flow inside the reactor 40, and the concentration mechanism of the solid is kept high. 41.
[0034]
That is, a fluid having a high solid concentration can be selectively collected in the vicinity of the lower center of the reactor 40, and the solid concentration of the fluid flowing through the throttle mechanism 41 is changed to an average solid of the processing fluid in the reactor. It can be increased compared to the object concentration.
[0035]
FIG. 4 is a diagram showing a cross-sectional shape of the diaphragm mechanism of the first embodiment shown in FIG. In the first embodiment shown in FIG. 1, the throttling mechanism 41 is constituted by a divergent nozzle having a circular channel cross-sectional shape.
[0036]
As shown in FIG. 4, the pressure of the processing fluid at the inlet of the throttle mechanism is P0, the channel cross-sectional area of the portion where the channel cross-sectional area of the throttle mechanism is the smallest is A *, the pressure of the processing fluid at the outlet of the throttle mechanism is P, Let A be the cross-sectional area of the flow path at the outlet of the throttle mechanism. Note that the pressure P0 of the processing fluid at the inlet of the throttle mechanism is substantially equal to the pressure of the processing fluid inside the reactor.
[0037]
High-temperature and high-pressure water has to be handled as a compressible fluid because the density varies depending on pressure even at the same temperature. Then, the relationship between the pressure ratio P / P0 at the throttle mechanism outlet / inlet and the flow path cross-sectional area ratio A / A * at the throttle mechanism outlet / minimum channel cross-sectional area must follow the following equation (Equation 1). .
[0038]
[Expression 1]

[0039]
In (Equation 1), γ is the specific heat ratio of water, and is a value of 1.5 to 1.6 for high-temperature and high-pressure water used for the oxidation treatment of organic matter.
[0040]
FIG. 5 is a graph showing the relationship of (Equation 1) as P / P0 on the horizontal axis and A / A * on the vertical axis. As shown in FIG. 5, reducing the processing fluid using the throttle mechanism 41 means that P / P0 is smaller than 1. Therefore, the flow path cross-sectional area ratio A / A * is 1 at any pressure ratio. Must be bigger.
[0041]
That is, the throttle mechanism needs to have a shape such that the channel cross-sectional area at the outlet of the throttle mechanism is larger than the channel cross-sectional area of the portion with the smallest channel cross-sectional area.
[0042]
By making the flow path cross section of the throttle mechanism 41 into a divergent shape, the fluid temperature at the outlet of the throttle mechanism 41 is automatically lower than the fluid temperature at the inlet of the throttle mechanism 41 as a property of the compressible fluid. Therefore, the temperature of the fluid flowing through the back pressure device 50 is lower than the temperature of the fluid inside the reactor 40.
[0043]
In the first embodiment shown in FIG. 1 or FIG. 2, the throttle mechanism 41 shows a case where the flow path cross-sectional shape is circular. Any shape can be used.
[0044]
When the oxidation reaction in the reactor is performed in a supercritical state of water, for example, the temperature of the fluid after the reaction is about 380 ° C. and the pressure is about 22 MPa. If the back pressure device is not provided and the degree of pressure reduction is adjusted using a valve or the like, the movable part of the valve will be exposed to a high-temperature and high-pressure fluid. The reliability of the valve is lowered, and as a result, the reliability of the entire processing system is reduced.
[0045]
According to the first embodiment shown in FIG. 1, the throttle mechanism 41 is constituted by a divergent nozzle, the back pressure device 50 is provided in the throttle mechanism 41, and the gas phase portion from the gas-liquid separator 70 is connected to the valve 52. In this case, the degree of decompression, that is, the pressure of the back pressure device 50 can be adjusted by the valve 52.
[0046]
Since the temperature of the gas phase supplied from the gas-liquid separation 70 passes through the preheater 30, it is lower than the temperature of the fluid immediately after the reaction, the reliability of the valve 52 can be improved, and adjustment is easy. Further, since the diaphragm mechanism 41 does not have a movable part, it can function stably even under high temperature and high pressure conditions, and as a result, the reliability of the entire system can be improved.
[0047]
Further, since the pressure in the back pressure device 50 is reduced by the throttle mechanism 41, any pressure that can withstand a pressure lower than that of the reactor 40 may be used.
[0048]
In FIG. 1, other oxidizing agents such as air may be used instead of oxygen.
[0049]
FIG. 6 is a system diagram showing an organic matter oxidation treatment system according to a second embodiment of the present invention. This configuration differs from FIG. 1 in that the reactor is composed of a reactor 40A and a reactor 40B, the reactors 40A and 40B are connected in series, and the fluid in the reactor 40A is A part is introduced into the back pressure unit 50 through the throttle mechanism 41A, and the remaining part is introduced into the reactor 40B. The fluid in the reactor 40B is partly introduced into the back pressure unit 50 through the throttle mechanism 41B, and the remaining part. Is the same as that of the embodiment shown in FIG.
[0050]
According to the second embodiment shown in FIG. 6, even when there is a solid matter that is not discharged by the throttle mechanism 41A provided in the preceding reactor 40A, the throttle mechanism 41B provided in the latter reactor 40B. Solids can be discharged.
[0051]
Thus, the solids removal efficiency can be increased by connecting a reactor equipped with a throttling mechanism in series.
[0052]
In the embodiment shown in FIG. 6, the throttle mechanisms respectively provided in the two reactors are communicated with one back pressure device, but individual back pressure devices may be provided in each reactor.
[0053]
In the embodiment shown in FIG. 6, the case where two reactors are connected in series is shown. However, by connecting three or more reactors in series, better solids separation can be achieved. It can be carried out.
[0054]
FIG. 7 is a system diagram showing an organic matter oxidation treatment system according to a third embodiment of the present invention. The processing system of the third embodiment shown in FIG. 7 includes an organic substance tank 10, an organic substance supply pump 11, an oxygen tank 20, an oxygen supply pump 21, an oxygen supply valve 22, and a preheater 30. The reactors 40A and 40B, the throttle mechanisms 41A and 41B, the valves 42A and 42B, the valves 43A and 43B, the back pressure devices 50A and 50B, the dust collector 60, and the back pressure device and the dust collector. It consists of valves 51A and 51B, a gas-liquid separator 70, and valves 52A and 52B communicating with the gas-liquid separator and the back pressure device.
[0055]
The water-containing organic substance 10 </ b> A stored in the organic substance tank 10 is introduced into the preheater 30 by the organic substance supply pump 11. On the other hand, the oxygen 20 </ b> A stored in the oxygen tank 20 is supplied by the oxygen supply pump 21 and mixed with the organic matter preheated by the preheater 30. The organic matter mixed with the oxygen 20A is introduced into a system including the reactor 40A and / or a system including the reactor 40B.
[0056]
In the system including the reactor 40A, when the valves 42A and 43A and the valves 51A and 52A are open, the organic matter mixed with the oxygen 20A is introduced into the reactor 40A and subjected to an oxidation reaction under high temperature and high pressure.
[0057]
A part of the fluid after the reaction is introduced into the back pressure unit 50A through the throttle mechanism 41A, and the remaining part is introduced into the preheater 30 through the valve 43A. The fluid after the reaction introduced into the preheater 30 and heat-exchanged with the organic matter before the reaction is introduced into the gas-liquid separator 70 and separated into the gas phase and the liquid phase, and then the gas phase portion is connected to the valve 52A. To the back pressure device 50A.
[0058]
In the back pressure device 50A, the reacted fluid introduced into the back pressure device through the throttle mechanism 41A is decompressed to a pressure approximately equal to the gas phase generated from the gas-liquid separator 70. By reducing the pressure, the boiling point of the water in the fluid after the reaction treatment decreases, the water evaporates, and the fluid after the reaction is separated into water vapor and solid matter.
[0059]
The separated water vapor and solid matter are introduced into a dust collector 60 communicated with the back pressure device 50A and the valve 51A, and the solid content is captured and removed by the dust collector 60.
[0060]
In the system including the reactor 40B, when the valves 42B and 43B and the valves 51B and 52B are open, the organic matter mixed with the oxygen 20A is introduced into the reactor 40B and subjected to an oxidation reaction under high temperature and high pressure.
[0061]
A part of the fluid after the reaction is introduced into the back pressure unit 50B through the throttle mechanism 41B, and the remaining part is introduced into the preheater 30 through the valve 43B. The fluid after the reaction introduced into the preheater 30 and heat-exchanged with the organic matter before the reaction is introduced into the gas-liquid separator 70 and separated into the gas phase and the liquid phase, and then the gas phase portion is connected to the valve 52B. To the back pressure device 50B.
[0062]
In the back pressure device 50 </ b> B, the reacted fluid introduced into the back pressure device through the throttle mechanism 41 </ b> B is decompressed to a pressure approximately equal to the gas phase generated from the gas-liquid separator 70. By reducing the pressure, the boiling point of the water in the fluid after the reaction treatment decreases, the water evaporates, and the fluid after the reaction is separated into water vapor and solid matter.
[0063]
The separated water vapor and solid matter are introduced into a dust collector 60 communicated with the back pressure device 50B via the valve 51B, and the solid content is captured and removed by the dust collector 60.
[0064]
According to the third embodiment shown in FIG. 7, it is possible to increase the throughput of organic matter by operating both the system including the reactor 40A and the system including the reactor 40B.
[0065]
In addition, when one of the system including the reactor 40A and the system including the reactor 40B stops the reaction and requires maintenance and inspection work such as replacement of parts, the other system is operated. Even during maintenance and inspection work, processing can be performed without stopping the entire system, and the reliability of the system can be improved.
[0066]
In the embodiment shown in FIG. 7, the case where two systems including reactors are provided in parallel is shown. However, by connecting three or more systems including reactors in parallel, further reliability can be obtained. A highly reliable system can be configured.
[0067]
FIG. 8 is a system diagram showing an organic matter oxidation treatment system according to a fourth embodiment of the present invention. This configuration differs from FIG. 7 in that the dust collector is composed of a dust collector 60A and a dust collector 60B, and the dust collector 60A is provided in communication with the back pressure device 50A via the valve 51A. The dust collector 60B is the same as the embodiment shown in FIG. 7 except that it is provided in communication with the back pressure device 50B via the valve 51B.
[0068]
According to the fourth embodiment shown in FIG. 8, even if maintenance or inspection work is required in one of the dust collectors 60A or 60B due to a decrease in dust collection capacity or the like, a system including the other dust collector By operating the system, it is possible to simultaneously perform processing of organic matter, maintenance, and inspection without stopping the entire system, so that a highly reliable system can be configured.
[0069]
FIG. 9 is a system diagram showing an organic matter oxidation treatment system according to a fifth embodiment of the present invention. This configuration differs from the first embodiment shown in FIG. 1 in that the steam D after the solid matter is removed by the dust collector 60 is introduced into the oxygen preheater 80, and the steam D and oxygen 20A are introduced. In other respects, the oxygen 20A is preheated by exchanging heat, and the rest is the same as the embodiment shown in FIG.
[0070]
In the oxidation treatment of organic matter using high-temperature water, in order to perform a good oxidation reaction in the reactor, it is necessary to preheat the organic matter to a certain temperature before introducing the organic matter into the reactor.
[0071]
According to the fifth embodiment shown in FIG. 9, the oxygen 20A is preheated by exchanging heat with water vapor supplied from the dust collector in the oxygen preheater 80, so that the oxygen 20A and the organic matter are mixed. A decrease in temperature due to mixing can be prevented, and a favorable oxidation reaction can be performed.
[0072]
Further, according to the present embodiment, since it is not necessary to input energy from the outside in order to preheat the oxygen 20A, it is possible to configure a self-sustaining operation type system with high energy use efficiency.
[0073]
【The invention's effect】
According to the present invention, in an organic matter oxidation treatment system using high-temperature water, the reactor is provided with a throttling mechanism, and further provided with a back pressure device, so that the reaction treatment water containing solid matter is continuously removed from the reactor. The solids can be discharged and continuously removed. Thereby, an oxidation treatment system can be operated efficiently.
[0074]
In addition, the throttling mechanism that discharges the reaction water containing the solid matter from the reactor does not have a movable part and functions stably even under high temperature and high pressure, so that the reliability of the entire processing system can be improved.
[Brief description of the drawings]
FIG. 1 is a system diagram showing an oxidation treatment system according to a first embodiment of the present invention.
FIG. 2 is a cross-sectional view showing an example of the reactor of FIG.
FIG. 3 is a top view showing an example of the reactor of FIG. 1;
4 is a schematic view showing the shape of the aperture mechanism of FIG. 1. FIG.
FIG. 5 is a graph showing channel cross-sectional area conditions of the throttle mechanism.
FIG. 6 is a system diagram showing an oxidation treatment system according to a second embodiment of the present invention.
FIG. 7 is a system diagram showing an oxidation treatment system according to a third embodiment of the present invention.
FIG. 8 is a system diagram showing an oxidation treatment system according to a fourth embodiment of the present invention.
FIG. 9 is a system diagram showing an oxidation processing system according to a fifth embodiment of the present invention.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 10 ... Organic substance tank, 10A ... Hydrous organic substance, 11 ... Organic substance supply pump, 20 ... Oxygen tank, 20A ... Oxygen, 21 ... Oxygen supply pump, 30 ... Preheater, 40, 40A, 40B ... Reactor, 41, 41A , 41B ... throttle mechanism, 50, 50A, 50B ... back pressure, 60, 60A, 60B ... dust collector, 70 ... gas-liquid separator, 80 ... oxygen preheater.

Claims (5)

  In an organic matter oxidation treatment system for oxidizing an organic matter in a fluid under high temperature and high pressure using water as a solvent, a reactor for oxidizing the fluid containing the organic matter and oxygen or an oxidizing agent under the high temperature and high pressure, A throttling mechanism provided in a reactor for discharging the oxidized processing fluid, and reducing the discharged processing fluid to approximately the same pressure as the gas supplied from a gas supply device to evaporate moisture and thereby vapor and solid An organic matter oxidation treatment system comprising a back pressure device that separates the product into a product.   2. The organic matter oxidation treatment system according to claim 1, wherein a dust collector for removing the separated solid matter is provided in communication with the back pressure device.   2. The organic oxidation system according to claim 1, wherein the gas supply device includes a gas-liquid separator or an air compressor that separates the processing fluid into a gas phase and a liquid phase.   2. The organic matter oxidation treatment system according to claim 1, wherein the throttle mechanism is configured by a divergent nozzle.   2. The organic matter oxidation treatment system according to claim 1, further comprising a preheater that heats the oxygen or the oxidizing agent by exchanging heat with water vapor generated by the back pressure device.

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