WO2020156336A1 - 超临界水氧化处理放射性有机固体废物 - Google Patents

超临界水氧化处理放射性有机固体废物 Download PDF

Info

Publication number
WO2020156336A1
WO2020156336A1 PCT/CN2020/073313 CN2020073313W WO2020156336A1 WO 2020156336 A1 WO2020156336 A1 WO 2020156336A1 CN 2020073313 W CN2020073313 W CN 2020073313W WO 2020156336 A1 WO2020156336 A1 WO 2020156336A1
Authority
WO
WIPO (PCT)
Prior art keywords
liquid
reactor
supercritical water
end plate
present disclosure
Prior art date
Application number
PCT/CN2020/073313
Other languages
English (en)
French (fr)
Inventor
张振涛
陈艳
刘刈
彭琳
龙泊康
张羽
任韧
孙润杰
李睿之
李振毅
张立军
张兴旺
骆永志
聂鹏
张卫亭
张建国
王海云
邱文苹
Original Assignee
中国原子能科学研究院
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from CN201910108896.8A external-priority patent/CN109772543B/zh
Priority claimed from CN201910109483.1A external-priority patent/CN109848182B/zh
Priority claimed from CN201910108898.7A external-priority patent/CN109647319B/zh
Priority claimed from CN201910108862.9A external-priority patent/CN109851029B/zh
Priority claimed from CN201910108890.0A external-priority patent/CN109851030B/zh
Application filed by 中国原子能科学研究院 filed Critical 中国原子能科学研究院
Priority to EP20748407.2A priority Critical patent/EP3919446A4/en
Publication of WO2020156336A1 publication Critical patent/WO2020156336A1/zh

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C02F11/08—Wet air oxidation
    • C02F11/086—Wet air oxidation in the supercritical state
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/008—Processes carried out under supercritical conditions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C18/00—Disintegrating by knives or other cutting or tearing members which chop material into fragments
    • B02C18/06—Disintegrating by knives or other cutting or tearing members which chop material into fragments with rotating knives
    • B02C18/14—Disintegrating by knives or other cutting or tearing members which chop material into fragments with rotating knives within horizontal containers
    • B02C18/142—Disintegrating by knives or other cutting or tearing members which chop material into fragments with rotating knives within horizontal containers with two or more inter-engaging rotatable cutter assemblies
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C18/00—Disintegrating by knives or other cutting or tearing members which chop material into fragments
    • B02C18/06—Disintegrating by knives or other cutting or tearing members which chop material into fragments with rotating knives
    • B02C18/16—Details
    • B02C18/22—Feed or discharge means
    • B02C18/2216—Discharge means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C18/00—Disintegrating by knives or other cutting or tearing members which chop material into fragments
    • B02C18/06—Disintegrating by knives or other cutting or tearing members which chop material into fragments with rotating knives
    • B02C18/16—Details
    • B02C18/18—Knives; Mountings thereof
    • B02C2018/188—Stationary counter-knives; Mountings thereof
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/006—Radioactive compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/02—Fluid flow conditions
    • C02F2301/026—Spiral, helicoidal, radial
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/26—Reducing the size of particles, liquid droplets or bubbles, e.g. by crushing, grinding, spraying, creation of microbubbles or nanobubbles
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids

Definitions

  • the invention relates to the field of solid waste treatment, in particular to a supercritical water oxidation system and a solid waste treatment method.
  • radioactive waste is increasing. If it is discharged without treatment or improper treatment, the environment will suffer radioactive pollution. It not only affects the growth of animals and plants, deteriorates water bodies, but also harms human health, and even has adverse effects on offspring.
  • Supercritical water oxidation is a new type of wet oxidation technology.
  • the organic matter is oxidatively decomposed into water, carbon dioxide, nitrogen and other gases, and the radionuclides contained in it are converted into inorganic salts, thereby completing the evaporation of organic solvents.
  • Liquid treatment Generally, supercritical water refers to water in a special state with a temperature exceeding 374°C and a pressure exceeding 22Mpa. In the supercritical water state, the organic waste and oxygen are completely miscible in the supercritical water system. When the temperature of the supercritical water exceeds 550°C, the solubility of inorganic salts in it is zero. Utilizing this performance of supercritical water, organic matter can be converted into carbon dioxide, water and inorganic salts, and the feature of inorganic salts having zero solubility above 550°C can be used to separate radioactive elements.
  • the treatment process of the supercritical water oxidation reactor is generally to directly mix the oxidant and the waste in the reactor, and then complete the reaction after the temperature of the oxidant and the waste reaches a certain temperature.
  • the waste will not only lower the temperature of the reaction zone, but also cause the waste to have a long reaction time in the supercritical water oxidation reactor and reduce the reaction efficiency.
  • the treatment of solid radioactive waste generally adopts the method of concentration reduction and isolation from the environment (such as burying, etc.).
  • the use of supercritical water oxidation and decomposition technology is the current focus of research on organic waste treatment, it has not been possible to perform supercritical water oxidation on solid waste at home and abroad.
  • the radioactive organic waste cannot be shredded to a sufficiently small particle size.
  • the size of the fragments obtained from the crushing of solid combustibles at home and abroad is often larger than 5mm.
  • due to the radioactive contamination of radioactive organic waste there is basically no shredding and grinding process for radioactive solid organic waste. This will undoubtedly affect the implementation of subsequent supercritical water oxidation treatment technology.
  • the second reason is the lack of protection technology for high temperature and high pressure equipment. Therefore, it is very important to develop protection technologies that can be applied to high temperature and high pressure reaction equipment.
  • the object of supercritical water oxidation reactor is liquid waste. It is difficult to perform supercritical water oxidation treatment of solid waste, and it cannot solve the problem of volume reduction and harm reduction of radioactive solid combustible waste such as nuclear power plants and other nuclear facilities.
  • the supercritical water equipment system does not form an integrated machine. Supercritical water oxidation, effluent purification, and protective equipment are completed by different equipment. The system integration is insufficient, resulting in supercritical water equipment not being promoted and applied in the form of industrial products. Furthermore, the reaction temperature of the usual supercritical water technology is generally low, the general temperature is 500 ⁇ 600°C, which is lower than the minimum temperature (about 700°C) required for complete pyrolysis and gasification of organic matter, and it cannot reach the difficult-to-degrade organic matter. (Amines, etc.) are completely inorganic, which makes the advantages of supercritical water oxidation insufficient.
  • embodiments of the present invention provide a supercritical water oxidation system and a solid waste treatment method.
  • a supercritical water oxidation reactor including a shell, a chamber for providing a reaction zone is formed inside, and the shell is provided with at least a slurry inlet, an oxidant inlet, and a discharge port; heating A device for increasing the temperature of the chamber; a spiral loop tube is arranged in the chamber, one end of the spiral loop tube is in communication with the slurry inlet, wherein the slurry is introduced into the spiral loop tube from the slurry inlet, It flows along the pipe of the spiral loop pipe and flows out from the other end of the spiral loop pipe; wherein, after the slurry flows out from the other end of the spiral loop pipe, it mixes with the oxidant flowing into the chamber from the oxidant inlet and generates Oxidation reaction.
  • the supercritical water oxidation reactor further includes a turn-back tube disposed in the chamber, the turn-back tube includes an inner tube with two ends open and an outer tube with one end open, and the outer tube is sleeved in the inner tube. Outside of the tube, the inner tube communicates with the oxidant inlet.
  • the above-mentioned turn-back tube is disposed at a central axis position of the above-mentioned chamber.
  • the supercritical water oxidation reactor further includes a stirrer, and the stirrer includes a rotating shaft.
  • the rotating shaft passes through the housing and extends into the cavity, and/or the rotating shaft passes through the discharge port and extends into the above-mentioned chamber. Chamber.
  • the housing includes a first end wall, a side wall, and a second end wall opposite to the first end wall, wherein the slurry inlet is provided on the side wall, and the oxidant inlet It is arranged on the first end wall, and the agitator and the discharge port are arranged on the second end wall.
  • the supercritical water oxidation reactor further includes an inner lining, which is arranged in the chamber, wherein the spiral loop pipe is wound around the outer wall of the inner lining, and the inner lining is aluminized and shot peened.
  • the thermal barrier coating includes multiple aluminum layers and multiple aluminum oxide layers alternately arranged.
  • the supercritical water oxidation reactor further includes a cooling device, arranged on the side wall, for cooling the reaction product generated in the chamber; wherein the heating device and the cooling device are arranged side by side on the On the side wall, and the distance between the heating device and the first end wall is smaller than the distance between the cooling device and the first end wall.
  • Another aspect of the present disclosure provides a method for processing radioactive organic waste using the above-mentioned supercritical water oxidation reactor, the method comprising preheating the above-mentioned chamber by the above-mentioned heating device; the temperature in the above-mentioned chamber reaches a first temperature At this time, the target solution is fed into the chamber through the slurry inlet, and the chamber is continued to be heated until the temperature in the chamber reaches the second temperature; the slurry of the radioactive organic waste is fed into the spiral through the slurry inlet
  • the circulation pipe flows along the pipe of the spiral circulation pipe and flows out from the other end of the spiral circulation pipe; after the radioactive organic waste slurry flows out from the other end of the spiral circulation pipe, it enters the cavity from the oxidant inlet
  • the oxidant in the chamber mixes and an oxidation reaction occurs.
  • the above method further includes that when the supercritical water oxidation reactor includes a turn-back tube, the oxidant first enters the turn-back tube from the oxidant inlet, and then passes through the inner tube and the outer tube of the turn-back tube in sequence. After that, enter the chamber from the opening of the outer tube.
  • the above-mentioned stirrer is used to stir the oxidation product obtained after the oxidation reaction occurs;
  • the oxidation product is discharged from the discharge port, wherein the temperature when the oxidation product is discharged from the discharge port is between 150°C and 300°C, and the second temperature is greater than or equal to 600°C .
  • the shredder includes a material guide box, a shredding device, a material box and a colloid mill which are connected to each other and arranged in sequence.
  • the guide box is used to introduce solid materials and make the solid materials fall along the axial direction of the guide box.
  • the shredding device includes a cutter capable of rotating under the drive of an external force, and the shredding device is used for cutting the solid material falling in the axial direction of the guide box into pieces by the cutter.
  • the material box is used to drive the broken pieces falling from the shredding device to move through the flowing liquid introduced into the material box.
  • the bottom of the material box is provided with a sieve plate including a plurality of sieve holes, which is used to filter out part of the liquid and the fragments whose size is smaller than the size of the plurality of sieve holes.
  • the colloid mill is set under the sieve plate, and is used to grind the fragments from the filter box into a slurry.
  • the above-mentioned shredding device includes a cutting assembly including a fixed cylinder, a rolling cylinder, and a plurality of first cutters.
  • the axial direction of the fixed cylinder is perpendicular to the axial direction of the guide box
  • the fixed cylinder includes a first side wall
  • the first side wall is provided with a corresponding first opening and a second opening, which are respectively used for communication Guide box and material box.
  • the rolling cylinder is arranged in the fixed cylinder along the axial direction of the fixed cylinder.
  • the rolling cylinder includes a second side wall, and the distance between the second side wall and the first side wall corresponds to the size of the solid material.
  • a plurality of first cutting knives are uniformly arranged on the outer surface of the second side wall along the circumferential direction of the rolling cylinder to form a first knife array for dropping into the first side wall and the first side wall along the axial direction of the guide box.
  • the solid material between the two side walls is cut into blocks. Wherein, the distance between two adjacent first cuts in the first knife array is set to correspond to the size of the block.
  • the above-mentioned shredding device further includes a shredding component.
  • the pulverizing component is arranged at a position between the rolling cylinder and the material box in the fixed cylinder, and the pulverizing component includes a second cutter for cutting the falling block into pieces.
  • the distance between the crushing component and the first side wall is greater than the preset distance, so that the fragments can fall into the bin.
  • the above-mentioned second cutter includes an axial cutter and a radial cutter.
  • the axial cutter is arranged along the axial direction of the guide box; the radial cutter is arranged in a direction perpendicular to the axial direction of the guide box and the axial direction of the fixed cylinder.
  • the radial cutter is coaxial with the axial direction, and the radial cutter is located between the axial cutter and the material box.
  • the axial cutter and the radial cutter are configured to rotate around a coaxial central axis under the action of the first external force.
  • the above-mentioned dicing assembly further includes a plurality of third cutters.
  • the plurality of third cutting knives are uniformly arranged on the inner surface of the first side wall along the circumferential direction of the fixed cylinder to form a second knife array.
  • the above-mentioned rolling cylinder can be rotated around its central axis under the action of the second external force, so that the solid material falling between the first side wall and the second side wall along the axial direction of the guide box can move between the first knife array and the second side wall. It was cut into lumps under the action of the two knife array.
  • the aforementioned roller includes at least one set of rollers.
  • Each set of rollers in the at least one set of rollers includes two opposing rollers.
  • the side walls of the two opposing rollers are each formed with a first knife array, and the two opposing rollers can be controlled by the second external force. Drive down to rotate in the opposite direction. Among them, the distance between two opposite rollers is smaller than the size of the solid material.
  • the plurality of first cutting knives and/or the plurality of second cutting knives are polygonal knives; and/or, the distance between two adjacent first cutting knives in the first knife array And/or the distance between two adjacent third cutters in the second knife array is in the order of decimeters.
  • the aforementioned guide box includes a pair of third side walls that are oppositely disposed.
  • Each third side wall of the pair of third side walls is provided with a plurality of nozzles for introducing liquid, so that the solid material is guided along by the liquid introduced by the plurality of nozzles of the pair of third side walls.
  • the axial direction of the material box falls.
  • each third side wall is parallel to the axial direction of the fixed cylinder and the axial direction of the guide box.
  • the above-mentioned solid material shredder further includes a flow guiding device.
  • the diversion device is used to drive the flowing liquid introduced into the material box to flow, and divert the fragments and liquid that are not filtered out of the material box to the guide box.
  • the width of the fragment in any one direction is less than 5 mm; and/or, the particle size of the slurry is less than 50 ⁇ m.
  • a protective device for reaction equipment which includes a pair of protective end plates and a protective component that are arranged oppositely.
  • the protection component is arranged between a pair of protection end plates, and the protection component includes an outer protection layer, an inner protection layer and a cooling layer.
  • the outer protective layer and a pair of protective end plates enclose a first space.
  • the inner protective layer is arranged in the first space and encloses a pair of protective end plates to form a second space for accommodating the reaction equipment.
  • the inner protective layer is provided with a plurality of diversion holes along the connection direction of the pair of protective end plates, which are used to guide the release of the reaction equipment between the outer protective layer and the inner protective layer.
  • the cooling layer is sandwiched between the inner protective layer and the outer protective layer, and the cooling layer includes a liquid pipeline capable of storing liquid.
  • the protection component is configured as follows: when the reaction device in a working state is accommodated in the second space, liquid is stored in the liquid pipeline, and the first space is a closed space.
  • the aforementioned pair of protective end plates includes a first protective end plate and a second protective end plate.
  • the first protective end plate has a first liquid inlet, a first liquid outlet, and a first liquid passage connecting the first liquid inlet and the first liquid outlet.
  • the first liquid inlet can be opened or closed under the action of an external force, and the first liquid
  • the outlet is in communication with the liquid pipeline, and the first protective end plate is configured to allow the liquid introduced from the first liquid inlet to flow through the first liquid passage and flow into the liquid from the first liquid outlet when the first liquid inlet is open Pipeline.
  • the second protective end plate has a second liquid inlet, a second liquid outlet, and a second liquid passage connecting the second liquid inlet and the second liquid outlet.
  • the second liquid outlet can be opened or closed under the action of an external force.
  • the liquid pipeline is in communication, and the second protective end plate is configured to allow the liquid in the liquid pipeline to flow out of the liquid pipeline from the second cooling liquid inlet and flow through the second liquid passage when the second liquid outlet is opened. Lead out the second coolant outlet.
  • the protective device is configured to: when the reaction device in the working state is accommodated in the second space, the first liquid inlet and the second liquid outlet are closed, and liquid is stored in the first liquid passage and the second liquid passage .
  • the first protective end plate of the pair of protective end plates has a first liquid inlet, a first liquid outlet, and a first liquid passage connecting the first liquid inlet and the first liquid outlet;
  • the second protective end plate of the protective end plate has a second liquid inlet, a second liquid outlet, and a second liquid passage connecting the second liquid inlet and the second liquid outlet;
  • the liquid pipeline includes a plurality of first pipelines,
  • the plurality of first pipelines extend in the connecting direction of the pair of protective end plates, and the plurality of first pipelines are periodically arranged in the direction perpendicular to the inner protective layer and the circumferential direction of the inner protective layer.
  • the plurality of first pipelines have opposite first ends and second ends, the first ends are in communication with the first liquid outlet, and the second ends are in communication with the second liquid inlet.
  • the aforementioned liquid pipeline further includes a plurality of second pipelines.
  • the plurality of second pipelines extend in the circumferential direction of the inner protective layer, and the plurality of second pipelines are periodically arranged in the connection direction of the pair of protective end plates and the direction perpendicular to the inner protective layer.
  • the plurality of second pipelines are in communication with the plurality of first pipelines via a plurality of pipeline connectors, and the protective device is configured to allow the liquid introduced from the first liquid inlet to flow into the first liquid passage, the first The pipeline and the second pipeline.
  • the above-mentioned first protective end plate includes a first end plate, a second end plate and a first cylinder.
  • the first cylinder is provided between the first end plate and the second end plate to enclose a first liquid passage between the first end plate and the second end plate, and the first liquid inlet is provided on the first cylinder
  • the first liquid outlet is arranged on the second end plate, and the second end plate is close to the second protective end plate relative to the first end plate.
  • the aforementioned second protective end plate includes a third end plate, a fourth end plate, and a second cylinder.
  • the second cylinder is provided between the third end plate and the fourth end plate to enclose a second liquid passage between the third end plate and the fourth end plate, and the second liquid outlet is provided on the first cylinder
  • the second liquid outlet is arranged on the third end plate, and the third end plate is close to the first protective end plate relative to the fourth end plate.
  • the thickness of the first end plate and/or the second end plate is 30 mm to 70 mm, and the height of the second cylinder is 30 mm to 70 mm; and/or, the third end plate and/or The thickness of the fourth end plate is 30mm-70mm, and the height of the second cylinder is 30mm-70mm.
  • the above-mentioned multiple diversion holes are periodically arranged on the inner protective layer.
  • the thickness of the inner protective layer is 30 mm-50 mm; the thickness of the outer protective layer is 30 mm-50 mm; and/or the main material of the inner protective layer and/or the outer protective layer includes steel.
  • reaction system which includes the above-mentioned protective device for the reaction equipment and the reaction equipment.
  • the reaction equipment is placed in the second space enclosed by the inner protective layer of the protective device and a pair of protective end plates.
  • the aforementioned reaction device includes a supercritical water reaction device.
  • a supercritical water oxidation system which includes a water supply device for providing water and a target solution; an oxidizer supply device for providing an oxidizer for the supercritical water oxidation reaction; solid combustibles chopping and grinding
  • the slurry machine is used to grind the solid combustibles into slurry; the supercritical water oxidation reactor is used to receive the slurry obtained after the solid combustibles are ground, the above-mentioned oxidant, the above-mentioned water and the above-mentioned target solution, and provide supercritical water
  • the reaction zone of the critical water oxidation reaction separation equipment for separating the effluent of the supercritical water oxidation reactor.
  • the above-mentioned supercritical water oxidation reactor includes a first shell in which a chamber for providing the above-mentioned reaction zone is formed, and at least a slurry inlet, an oxidant inlet, and a discharge are provided on the first shell A heating device for increasing the temperature of the chamber; a spiral loop pipe is arranged in the chamber, one end of the spiral loop pipe is connected to the slurry inlet, wherein the spiral loop pipe is set to make the slurry from After the slurry inlet is introduced into the spiral loop tube, it flows along the pipe of the spiral loop tube, flows out from the other end of the spiral loop tube, and mixes with the oxidant flowing into the chamber from the oxidizer inlet to cause an oxidation reaction.
  • the above-mentioned supercritical water oxidation reactor further includes a turn-back tube disposed in the above-mentioned chamber, and the above-mentioned turn-back tube includes an inner tube with open ends and an outer tube with one end open, and the outer tube is sleeved on the Outside of the inner tube, the inner tube communicates with the oxidant inlet.
  • the above-mentioned turn-back tube is disposed at a central axis position of the above-mentioned chamber.
  • the supercritical water oxidation reactor further includes a stirrer, the stirrer includes a rotating shaft, the rotating shaft passes through the first housing and extends into the cavity, and/or the rotating shaft passes through the discharge port Extends into the cavity; an inner lining is arranged in the cavity, wherein the spiral circulation pipe is wound around the outer wall of the inner lining.
  • the above-mentioned separation device includes an evaporation tank for receiving the effluent of the above-mentioned supercritical water oxidation reactor, wherein the above-mentioned effluent is a multi-phase mixture, and the above-mentioned evaporation tank is provided with a first cooling plate
  • the first cooling coil is used to stabilize the temperature of the solution in the evaporation tank within the target temperature range after the multi-phase mixture flows into the evaporation tank, and the slag discharge port is used to discharge the The solid substance in the phase mixture
  • the cooling inner barrel includes a second cooling coil and a condensing pool, the second cooling coil is used to cool the vapor evaporated in the evaporation pool, and the condensing pool is used to receive the second cooling coil
  • the liquid substance obtained after cooling the steam, the condensation pool is provided with a drain for discharging the liquid substance, wherein the barrel wall of the cooling inner barrel is provided with a plurality of holes for the steam evaporated
  • a sleeve for receiving the polymorphic phase mixture is provided in the evaporation tank, and a plurality of small holes are distributed on the pipe wall of the sleeve, and the polymorphic phase mixture is dispersed and discharged through the plurality of small holes. Into the above evaporation pool.
  • the aforementioned separation device further includes a back pressure valve, wherein one end of the back pressure valve is connected to the sleeve through a pipe, and the other end of the back pressure valve is used to connect to the supercritical water oxidation reactor through a pipe.
  • the discharge port is connected; and/or the above-mentioned exhaust port is equipped with an online volatile organic monitor; and/or the above-mentioned evaporation tank is equipped with a level gauge; and/or the above-mentioned evaporation tank is equipped with a pH meter; and/or the above-mentioned drainage
  • the mouth is equipped with an online chemical oxygen demand monitor.
  • Another aspect of the present disclosure provides a method for treating solid combustibles by using a supercritical water oxidation system, which includes raising the temperature of the chamber of the supercritical water oxidation reactor to a first temperature; Enter the above-mentioned chamber; enter the target solution into the above-mentioned chamber through the above-mentioned water supply device, and continue heating the above-mentioned chamber until the temperature in the above-mentioned chamber reaches the second temperature; through the above-mentioned solid combustibles chopping and grinding machine, the solid combustibles Grind to slurry, and input the slurry into the chamber, so that the slurry reacts with the oxidant to obtain an effluent; the effluent is fed into the outlet of the supercritical water oxidation reactor The aforementioned separation device; and the aforementioned effluent is separated by the aforementioned separation device.
  • the method further includes monitoring the COD value of the discharged liquid substance through an online chemical oxygen demand monitor provided on the separation device; and/or The volatile organic compound online monitor installed on the above separation equipment monitors the VOC value of the discharged gaseous substances; and/or the pH value of the solution in the evaporation tank in the above separation equipment is monitored by the pH meter installed on the above separation equipment; and/or The temperature of the solution in the evaporation tank in the separation device and/or the temperature in the cooling inner barrel is monitored by a thermometer set on the separation device.
  • the system includes a reactor, a protective device, an oxidant supply device and an organic material supply device.
  • the reactor includes a reactor shell, the reactor shell is provided with an oxidant feed port, an organic material feed port, and a feed port, and the reactor discharges the reaction product through the feed port.
  • the protective device includes an outer protective layer, a cooling layer and an inner protective layer.
  • the inner protective layer and the outer protective layer enclose a first space and a second space
  • the cooling layer includes a liquid pipeline capable of storing liquid
  • the liquid pipeline is arranged in the first space
  • the reactor is arranged in the second space
  • the discharge port of the reactor extends to the area in the first space except the area where the liquid pipeline is located, so that the reaction product discharged from the discharge port can be cooled by the liquid stored in the liquid pipeline.
  • the oxidant supply device is communicated with the oxidant feed port, and the organic matter feed device is communicated with the organic matter feed port.
  • the outer protective layer includes an outer sleeve and a pair of opposite side wall end plates
  • the inner protective layer includes a coaxial first cylinder and a pair of opposite second cylinders.
  • the cylinder is arranged between the pair of second cylinders and is coaxial with the pair of second cylinders.
  • the first cylinder includes the side wall of the first cylinder, and it is a structure with open ends.
  • Each second cylinder in a pair of second cylinders includes a first end plate and a second cylinder side wall.
  • the first end plate is a ring-shaped plate structure whose inner ring size matches the size of the first cylinder, and
  • the pair of second cylinders are fixedly connected to the first cylinder via the first end plate.
  • the side wall of the first cylinder, the first end plate and the outer sleeve enclose the first space
  • the first cylinder, the second cylinder and the pair of side wall end plates enclose the second space.
  • the above-mentioned liquid pipeline includes a plurality of double-layer sleeves extending along the connecting direction of a pair of side wall end plates, and the plurality of double-layer sleeves are periodically arranged in the radial direction of the outer sleeve and the circumferential direction of the outer sleeve.
  • each double-layer casing includes an outer casing and an inner casing.
  • the first end plate is provided with a plurality of first ports for communicating with the outer sleeves of the plurality of double sleeves respectively.
  • the second side wall of each of the above-mentioned pair of second cylinders has a first opening, one of the first openings serves as the first liquid inlet, and the other first opening serves as the first outlet. Liquid port.
  • the above-mentioned protective device is configured to: when the reactor set in the second space is in working condition, the liquid is circulatedly introduced from the first liquid inlet, and after flowing through the outer casing of a plurality of double casings, The first liquid outlet is led out to cool the reaction product discharged from the outlet.
  • each of the above-mentioned pair of second cylinders further includes a second end plate opposite to the first end plate, and a second end plate disposed between the first end plate and the second end plate.
  • the first opening is arranged on the side wall between the first end plate and the boundary plate.
  • a plurality of second interfaces are provided on the above-mentioned boundary plate, which are used to respectively communicate with the inner casings of the plurality of double casings.
  • the length of the inner sleeve is greater than the outer sleeve, and the second end plate is provided with a plurality of communication holes for connecting the inner sleeve with the second space.
  • the second end plate and the boundary plate have the same annular plate structure as the first end plate.
  • the aforementioned cooling layer further includes a plurality of gas pipelines and condensate collecting trays.
  • the condensate collecting tray is arranged between two adjacent sets of double-layer sleeves periodically arranged along the radial direction of the outer sleeve in the first space, and the condensate collecting tray is closed on the first surface near the discharge port. Structure, and the second disk surface far away from the discharge port is an open structure.
  • the condensate collecting pan has a plurality of grooves periodically arranged in the axial direction of the outer sleeve, and the plurality of grooves extend in a direction perpendicular to the connection line of the first disk surface and the second disk surface.
  • a plurality of gas pipelines are arranged at a plurality of grooves extending along the connecting direction of the first disc surface and the second disc surface.
  • the first end of the plurality of gas pipelines is an open structure near the first disc surface, and the first end close to the second disc surface has an open structure.
  • the second end is a closed structure, the second ends of the plurality of gas pipelines are higher than the second disc surface, and the plurality of gas pipelines have a plurality of air injection ports on the sidewalls higher than the second disc surface.
  • the outer protective layer is provided with a slag discharge port, a liquid discharge port and an exhaust port for discharging the residue in the reaction product and the condensate and waste gas obtained by cooling the reaction product.
  • the liquid discharge port is connected with the condensate collection tray.
  • the above-mentioned reactor housing includes a first end wall, a side wall of the housing, and a second end wall disposed opposite to the first end wall.
  • the oxidant feed port is provided on the first end wall
  • the discharge port is provided on the second end wall
  • the organic material feed port is provided on the side wall of the housing close to the second end wall.
  • the above-mentioned reactor also includes a plurality of organic matter conveying pipes and end loop pipes. A plurality of organic substance conveying pipes are extended and arranged in the reactor shell along the connecting direction of the first end wall and the second end wall.
  • the multiple organic substance conveying pipes include a first end and a second end opposite to the first end, and the first end of the organic substance conveying pipe is in communication with the organic substance inlet.
  • the end loop tube is arranged in the region of the reactor shell close to the first end wall, and the end loop tube is communicated with the second ends of the plurality of organic substance conveying tubes.
  • the end loop pipe is provided with a plurality of first discharge holes on the side wall close to the second end wall, and/or the plurality of organic substance conveying pipes are close to the central axis of the reactor and close to the first end wall.
  • a plurality of second discharging holes are provided on the side wall of.
  • the above-mentioned reactor further includes a third cylinder and a feed plate.
  • the third cylinder is sleeved on the outside of the plurality of organic substance conveying pipes and the end loop pipes, and the third cylinder includes a third end plate and a third cylinder side wall.
  • the third end plate has a first feed hole corresponding to the oxidant feed port.
  • the feed plate is arranged between the third end plate and the end ring pipe to form an oxidant transmission channel between the feed plate and the third cylinder, and the feed plate is provided with a plurality of second feed holes.
  • a second liquid inlet and a second liquid outlet are further provided on the side wall of the housing.
  • the above-mentioned reactor also includes an inner liner and a circulating sleeve, the inner liner is arranged between the side wall of the shell and the side wall of the third cylinder, and the circulating sleeve is spirally wound between the inner liner and the side wall of the shell.
  • the above-mentioned circulating sleeve includes a third end and a fourth end opposite, the third end is connected with the second liquid inlet, and the fourth end is connected with the second liquid outlet.
  • the above-mentioned reactor further includes a stirring assembly including a rotating shaft that passes through the reactor shell and the discharge port. And/or, the space enclosed by the reactor shell can be divided into a first area close to the oxidant feed port and a second area close to the organic material feed port and discharge port.
  • the above-mentioned reactor further includes a heating component and/or a cooling component, the heating component is arranged outside the first zone to increase the temperature in the reactor shell, and the cooling component is arranged outside the second zone to cool the oxidant and organic matter. reaction product. And/or, when the above-mentioned reactor is in an operating state, the center temperature of the first zone is 700°C to 800°C.
  • the above-mentioned organic substance supply device includes an organic substance supply assembly, a lye tank, a first peristaltic pump, a first high-pressure pump, and a first one-way valve.
  • the first peristaltic pump is connected with the lye tank
  • the first high-pressure pump is respectively connected with the lye tank and the first peristaltic pump
  • the first one-way valve is arranged between the first high-pressure pump and the organic material feed port.
  • the above-mentioned organic material supply device further includes a sucrose solution tank, a water tank, a second peristaltic pump, a second high-pressure pump, and a second one-way valve.
  • the second peristaltic pump is in communication with the sucrose solution tank, and the second high-pressure pump is respectively connected to the water tank and the second one-way valve.
  • the two peristaltic pumps are connected, and the second one-way valve is arranged between the second high-pressure pump and the organic material feed port.
  • the above-mentioned organic material supply assembly includes an organic material chopping and refining machine for shredding and grinding solid organic material into a slurry.
  • the organic matter shredding and refining machine includes an inverting box, a shearing knife and a colloid mill which are mutually connected and arranged in sequence.
  • the guide box is used to introduce solid organic matter and liquid, and the bottom of the guide box is provided with a diversion hole.
  • the shearing knife is arranged above the diversion hole at the bottom of the guide box, and is used to cut the falling solid organic matter into 1 ⁇ 5mm slag.
  • the colloid mill is used to grind the slag flowing out of the orifice into a slurry.
  • the shearing knife and the colloid mill are coaxial to rotate synchronously under the action of external force.
  • the above-mentioned shearing knife includes a primary shearing knife and a secondary shearing knife.
  • the primary shearing knife is used to cut solid organic matter into 10-50mm pieces, and the secondary shearing knife is used to crush The block is cut into 1 ⁇ 5mm slag, and the secondary shearing knife is set under the primary shearing knife.
  • the oxidant and the waste are directly mixed in a supercritical water oxidation reactor, and then the temperature of the oxidant and the waste reaches a certain temperature before the complete reaction occurs.
  • the organic slurry has a large molecular weight and a stable molecular space structure, it is difficult to oxidize in a short time.
  • the waste material imported from the outside will not only lower the temperature of the reaction zone, but also cause a long reaction time of the waste material in the supercritical water oxidation reactor and reduce the reaction efficiency.
  • a spiral loop tube is set in the chamber of the supercritical water oxidation reactor.
  • the slurry flows in the spiral loop tube. It can be fully preheated, heated up, and even thermally decomposed, thereby ensuring the pyrolysis time of the organic slurry, ensuring the completeness of the organic slurry for supercritical water oxidation, and improving the reaction efficiency.
  • the solid materials By introducing the liquid into the guide box, the solid materials can be shredded in the liquid environment, so the generation of aerosol can be avoided; and because the solid materials can fall along the axial direction driven by the introduced fluid, the liquid can be used Flow feeding without external force, so you can make full use of space and reduce the overall size of the equipment;
  • the large piece of material is cut into pieces by the knife array on the roller, and the small piece of material is chopped by the third cutting knife rotating at a high speed, so that the solid material can be chopped to the millimeter level, which solves the problem that the solid material cannot be crushed to The technical bottleneck of the millimeter level; and the filtered pieces are ground by a colloid mill, which can achieve the beneficial effects of small particle size and uniform particle size of the slurry.
  • the released substance ejected by the explosion of the reaction device can be introduced between the outer protective sleeve and the inner protective sleeve.
  • the pressure difference is applied.
  • the released material can burst the liquid pipeline and the liquid flows out, thereby cooling and reducing the released material, avoiding the damage to the environment caused by the released material being sprayed directly to the external environment;
  • the cooling layer can be integrated into a dense pipeline cage. Therefore, when the release is introduced into the cooling layer, the pipeline and the release can be increased.
  • the contact area and therefore can increase the speed of cooling and decompression of the release, and control the entire process of cooling and decompression within 100s, effectively preventing the impact of the release to the outer protective layer;
  • the uniform dispersion of the released material can be realized, and therefore the concentrated impact of the released material can be avoided, and the cooling and pressure reduction efficiency is further improved.
  • the supercritical water oxidation system of the present disclosure may be used to process solid combustible slurry.
  • solids if solids are directly fed into the supercritical water oxidation reactor, it will cause blockage in the supercritical water oxidation reactor.
  • This disclosure breaks through the technical bottleneck that the feed is liquid or gas at home and abroad, and the solids can be shredded and refined. After that, the particles of the slurry were lower than 50 ⁇ m, and the slurry was pumped into the supercritical water oxidation reactor.
  • obstacles were eliminated, and radioactive solids such as nuclear power plants and other nuclear facilities were solved. Volume reduction and harm reduction of combustible waste.
  • the supercritical water oxidation system of the embodiment of the present disclosure has an all-in-one machine that integrates the functions of supercritical reaction and reaction product cooling and separation, and no additional separator is required, thereby facilitating the popularization and application of supercritical water oxidation technology;
  • the liquid pipeline adopts double-layer casing, and through the design of the inner protective layer, the space between the inner casing of the double-layer casing and the outer casing can be isolated.
  • the cooling liquid is carried in the outer sleeve, while the inner sleeve is connected to the second space where the reactor is located.
  • the reactor explodes abnormally and ejects high-temperature and high-pressure organic releases, the releases can be introduced into the inner casing through the inner protective layer, isolated from the external environment of the protective device, and can flow through the outer casing.
  • the liquid is cooled down. Therefore, the supercritical water oxidation system of the embodiment of the present disclosure also integrates a protective function, which can effectively prevent abnormal releases from spraying out of the protective device, so the integration is high, and the damage of abnormal releases to the external environment can be effectively avoided;
  • the organic substance conveying pipe and the end loop pipe in the reactor can be uniformly introduced into the center chamber of the reactor from the end and side walls.
  • the design of the feed plate and the third cylinder body can ensure that the oxidant is uniformly introduced into the center chamber of the reactor from the end and side walls. Therefore, the organic matter and the oxidant can be fully contacted and mixed, so that the temperature of the center chamber of the reactor reaches 700°C to 800°C. Therefore, it can ensure that the advantages of supercritical water oxidation reaction are fully utilized, and it is beneficial to the complete pyrolysis and gasification of organic matter.
  • Fig. 1 schematically shows a schematic diagram of a supercritical water oxidation reactor according to an embodiment of the present disclosure
  • Figure 2 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure
  • Fig. 3 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure
  • FIG. 4 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure
  • Fig. 5 schematically shows a schematic diagram of a cooling device according to an embodiment of the present disclosure
  • FIG. 6 schematically shows a flow chart of using a supercritical water oxidation reactor to treat radioactive organic waste according to an embodiment of the present disclosure
  • Figure 7 schematically shows a front sectional view of a solid material shredder according to the first embodiment of the present disclosure
  • Figure 8 schematically shows a side sectional view of the solid material shredder according to the first embodiment of the present disclosure
  • Fig. 9 schematically shows a structural diagram of a shredding device according to an embodiment of the present disclosure.
  • FIGS. 10A to 10B schematically show the structure diagram of the first cutting knife/third cutting knife according to an embodiment of the present disclosure
  • FIG. 11A to 11B schematically show the structure diagram of a second cutter according to an embodiment of the present disclosure
  • Figure 12 schematically shows a front sectional view of a solid material shredder according to a second embodiment of the present disclosure
  • Figure 13 schematically shows a front sectional view of a solid material shredder according to a third embodiment of the present disclosure
  • FIG. 14 schematically shows a schematic structural diagram of the protective device of the reaction equipment according to the first embodiment of the present disclosure
  • Fig. 15A schematically shows a structural diagram of a first protective end plate in a pair of protective end plates according to an embodiment of the present disclosure
  • Fig. 15B schematically shows a schematic structural view of a second protective end plate in a pair of protective end plates according to an embodiment of the present disclosure
  • Fig. 16 schematically shows a structural diagram of a protective device of a reaction equipment according to a second embodiment of the present disclosure
  • FIG. 17A schematically shows a front cross-sectional view of the protective device of the reaction device with reference to FIG. 16;
  • FIG. 17B schematically shows a side sectional view of the protective device of the reaction equipment with reference to FIG. 16;
  • FIG. 18 schematically shows a schematic diagram of a supercritical water oxidation system according to an embodiment of the present disclosure
  • FIG. 19 schematically shows a flowchart of a method for treating solid combustibles by using a supercritical water oxidation system according to an embodiment of the present disclosure
  • Figure 20 schematically shows a schematic diagram of a supercritical water oxidation reactor according to an embodiment of the present disclosure
  • Figure 21 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure
  • Figure 22 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure
  • FIG. 23 schematically shows a schematic diagram of a cooling device 2206 according to an embodiment of the present disclosure
  • Figure 24 schematically shows a schematic diagram of a separation device according to an embodiment of the present disclosure
  • Fig. 25 schematically shows a schematic diagram of a cooling inner tub according to an embodiment of the present disclosure
  • Figure 26 schematically shows a schematic diagram of a sleeve according to an embodiment of the present disclosure
  • FIG. 27 schematically shows a structural diagram of a supercritical water oxidation system according to an embodiment of the present disclosure
  • Fig. 28 schematically shows the A-A sectional view in Fig. 27;
  • FIG. 29 schematically shows the structure diagram of the inner protective layer with reference to FIG. 27;
  • Figure 30 schematically shows a front cross-sectional view of a reactor according to an embodiment of the present disclosure
  • FIG. 31 schematically shows an enlarged view of the structure of the dashed frame area with reference to FIG. 30;
  • Fig. 32A schematically shows a left side view with reference to the B-B section in Fig. 31;
  • Fig. 32B schematically shows a right side view with reference to the B-B cross-sectional view in Fig. 31;
  • FIG. 33 schematically shows a structural diagram of an organic material feeding device according to an embodiment of the present disclosure
  • Figure 34 schematically shows a structural diagram of a rotary cutting refiner according to an embodiment of the present disclosure.
  • FIG. 35 schematically shows a top view of the rotary cutter refiner in reference to FIG. 34.
  • At least one of the “systems” shall include, but is not limited to, systems having A alone, B alone, C alone, A and B, A and C, B and C, and/or systems having A, B, C, etc. ).
  • At least one of the “systems” shall include, but is not limited to, systems having A alone, B alone, C alone, A and B, A and C, B and C, and/or systems having A, B, C, etc. ).
  • the embodiment of the present disclosure provides a supercritical water oxidation reactor, including a shell, a chamber for providing a reaction zone is formed inside, and at least a slurry inlet, an oxidant inlet, and a discharge port are provided on the shell; a heating device , Used to increase the temperature of the chamber; the spiral loop tube is set in the chamber, one end of the spiral loop tube is connected to the slurry inlet, where the slurry flows along the spiral loop tube after being introduced into the spiral loop tube from the slurry inlet , And flow out from the other end of the spiral loop tube; wherein, after the slurry flows out from the other end of the spiral loop tube, it mixes with the oxidant flowing into the chamber from the oxidant inlet and undergoes oxidation reaction.
  • FIG. 1 schematically shows a schematic diagram of a supercritical water oxidation reactor according to an embodiment of the present disclosure. It should be noted that FIG. 1 is only an example of a supercritical water oxidation reactor to which the embodiments of the present disclosure can be applied to help those skilled in the art understand the technical content of the present disclosure, but it does not mean the supercritical water oxidation reactor of the present disclosure
  • the water oxidation reactor cannot be constructed in other ways.
  • the supercritical water oxidation reactor 100 includes a shell 101, a heating device 102 and a spiral loop pipe 103.
  • a chamber for providing a reaction zone is formed inside the shell 101, and at least a slurry inlet 1011, an oxidant inlet 1012, and a discharge port 1013 are provided on the shell 101.
  • the housing 101 may include an outer shell and an inner shell (for example, the inner shell may be the inner liner 1014 in FIG. 1), and the shape, material, and size of the outer shell and the inner shell are not limited.
  • the main body of the housing 101 may be cylindrical, the inner diameter of the outer shell is 80-219 mm, and the length is 1000-9000 mm; the inner diameter of the inner shell is 40-133 mm, and the length is 1000-9000 mm.
  • the heating device 102 is used to increase the temperature of the chamber.
  • the type of the heating device 102 is not limited.
  • the heating device 102 may be a heating jacket.
  • a heating jacket can be sleeved on the outer wall of the housing 101, and heat is transferred to the cavity inside the housing 101 through heat conduction.
  • the present disclosure does not limit other heating methods.
  • the two ends of the outer shell of the supercritical water oxidation reactor 100 may be equipped with pressure gauges, the two ends and the middle of the inner shell may be equipped with temperature probes, and the heating jacket and the outer wall of the outer shell may be equipped with temperature probes.
  • the heating device 102 may cover a part of the outer wall of the housing 101.
  • the heating device 102 may be arranged on an outer wall corresponding to a predetermined area where the outlet of the spiral circulation pipe 103 is located, so as to cover a part of the housing 101.
  • the heating device 102 includes 4 heating jackets, covering the middle of the casing 101 to the area from the spiral loop pipe 103 to the outlet of the slurry.
  • the spiral loop pipe 103 is arranged in the chamber, and one end 1031 of the spiral loop pipe is in communication with the slurry inlet 1011. After the slurry is introduced into the spiral loop pipe 103 from the slurry inlet 1011, it flows along the pipe of the spiral loop pipe 103 and flows from the spiral loop pipe 103. The other end 1032 of the pipe flows out, wherein after the slurry flows out from the spiral loop pipe 1032, it mixes with the oxidant flowing into the chamber from the oxidant inlet 1012 and undergoes an oxidation reaction. It should be noted that the loop tube in the spiral loop tube 103 in FIG. 1 is only schematic, and the length and number of turns of the loop tube are not limited in this disclosure.
  • the spiral circulation pipe 103 can flow the organic slurry along the circulation pipe. On the one hand, it increases the degree of flow of the organic slurry and on the other hand increases the flow rate of the organic slurry, which can increase the heat of the organic slurry. Solution efficiency.
  • the spiral circulation pipe 103 may be disposed close to the inner wall of the housing 101. Specifically, in the case where the housing 101 includes an outer shell and an inner shell, the spiral circulation pipe 103 may be disposed between the outer shell and the inner shell. In order to increase the degree of flow of the organic slurry, the spiral loop pipe 103 can be wound around the inner shell for installation.
  • the inner shell may also be referred to as an inner liner. As shown in FIG. 1, the position of the inner liner may be set as shown in FIG.
  • the supercritical water oxidation reactor 100 of the present disclosure may be used to process solid combustible slurry.
  • thermal decomposition in the spiral loop tube 103 can be realized.
  • the supercritical water oxidation reaction can proceed.
  • the average temperature of supercritical water is 600°C
  • the pyrolysis of organic matter generally takes about 1 second.
  • the residence time of organic matter is at least 8s, and the effect is better than theoretically required.
  • the organic matter if the organic matter is directly fed, the organic matter will cool the temperature of the reaction zone and reduce the reaction effect.
  • the reaction temperature is 600°C
  • the pyrolysis time of the organic matter is about 1s
  • the reaction temperature is 550°C
  • the time required for the pyrolysis of the organic matter is 5min, which will reduce the reaction efficiency. It can be seen that, compared with the prior art, the present disclosure has a very fast response time and improves processing efficiency.
  • the oxidant and the waste are directly mixed in a supercritical water oxidation reactor, and then the temperature of the oxidant and the waste reaches a certain temperature before the complete reaction occurs.
  • the organic slurry has a large molecular weight and a stable molecular space structure, it is difficult to oxidize in a short time.
  • the waste input from the outside not only lowers the temperature of the reaction zone, but also results in a long reaction time of the waste in the supercritical water oxidation reactor and reduces the reaction efficiency.
  • a spiral loop tube is set in the chamber of the supercritical water oxidation reactor.
  • the slurry flows in the spiral loop tube. It can be fully preheated, heated up, and even thermally decomposed, thereby ensuring the pyrolysis time of the organic slurry, ensuring the completeness of the organic slurry for supercritical water oxidation, and improving the reaction efficiency.
  • Fig. 1 The reactor shown in Fig. 1 will be further described with reference to Figs. 2 to 5 in combination with specific embodiments.
  • Fig. 2 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure.
  • the supercritical water oxidation reactor 200 includes a shell 201, a heating device 202, a spiral loop pipe 203 and a turn-back pipe 204.
  • the shell 201 is provided with a slurry inlet 2011, an oxidant inlet 2012 and a discharge port 2013.
  • the spiral loop tube 203 includes one end 2031 of the spiral loop tube and the other end 2032 of the spiral loop tube.
  • housing 201, the heating device 202, and the spiral loop tube 203 in the embodiment of the present disclosure may refer to the description of FIG. 1 in the present disclosure.
  • the details are not repeated here.
  • the turn-back tube 204 is disposed in the chamber.
  • the turn-back tube 204 includes an inner tube 2041 with open ends and an outer tube 2042 with one end open.
  • the outer tube 2042 is sleeved outside the inner tube 2041, and the inner tube 2041 It is connected to the oxidant inlet 2012.
  • the oxidant after the oxidant is introduced from the oxidant inlet 2012, it passes through the inner tube 2041, then enters the outer tube 2042, and is finally discharged from an opening at one end of the outer tube 2042.
  • the turn-back tube 204 may be disposed at the central axis position of the chamber.
  • the shape, material, and size of the inner tube 2041 and the outer tube 2042 are not limited.
  • the diameter of the inner tube 2041 can be ⁇ 25 ⁇ 42mm
  • the wall thickness can be 4-6mm
  • the diameter of the outer pipe can be 42mm or more
  • the wall thickness can be 4-6mm
  • the length can be between 3000mm and 6000mm.
  • the size of the turn-back tube 204 is moderate, which can effectively reduce the production cost and is beneficial to market applications.
  • the turning-back tube can make the oxidant in the tube rise as much as possible, increasing the preheating time.
  • the turn-back tube is set at the central axis of the supercritical water reactor, so that the heating temperature can reach the highest.
  • the type of oxidant is not limited.
  • it can be liquid oxygen, hydrogen peroxide and so on.
  • Fig. 3 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure.
  • the supercritical water oxidation reactor 300 includes a shell 301, a heating device 302, a spiral loop pipe 303, a return pipe 304 and a stirrer 305.
  • the shell 301 is provided with a slurry inlet 3011, an oxidant inlet 3012, and a material outlet 3013.
  • the spiral loop tube 303 includes one end 3031 of the spiral loop tube and the other end 3032 of the spiral loop tube.
  • the turn-back tube 304 includes an inner tube 3041 with two ends open and an outer tube 3042 with one end open.
  • housing 301, the heating device 302, the spiral loop pipe 303, and the reentrant pipe 304 in the embodiment of the present disclosure may refer to the description of FIG. 1 and/or FIG. 2 in the present disclosure. For the sake of brevity of description, This will not be repeated here.
  • the agitator 305 includes a rotating shaft 3051, the rotating shaft 3051 extends through the housing 301 into the chamber, and/or the rotating shaft 3051 extends through the outlet 3013 into the chamber.
  • the agitator 305 may also include a rotor, a spacer sleeve, a magnetic block and other components required by the agitator (not shown in FIG. 3).
  • the positions of the slurry inlet 3011, the oxidant inlet 3012, and the discharge outlet 3013 are not limited.
  • the housing 301 includes a first end wall, a side wall, and a second end wall opposite to the first end wall.
  • the slurry inlet 3011 is provided on the side wall
  • the oxidant inlet 3012 is provided on the first end wall.
  • the agitator 305 and the discharge port 3013 are provided on the second end wall.
  • the discharge port 3013 may also be provided on the side wall.
  • the stirrer 305 may be a magnetic stirrer.
  • the supercritical water oxidation reactor 300 When the supercritical water oxidation reactor 300 is installed vertically, it can be installed at the bottom of the supercritical water oxidation reactor 300, mainly for Stir the sediment at the bottom of the reactor to prevent solid particles from depositing, compacting, and blocking the discharge port.
  • the supercritical water oxidation reactor 300 of the present disclosure may be used to process solid combustible slurry.
  • solids if solids are directly fed into the supercritical water oxidation reactor, it will cause blockage in the supercritical water oxidation reactor.
  • This disclosure breaks through the technical bottleneck that the feed is liquid or gas at home and abroad, and the solids can be shredded and refined. After that, the particles of the slurry are lower than 50 ⁇ m, and the slurry is pumped into the supercritical water oxidation reactor, which eliminates obstacles to prevent large particles from depositing inside the supercritical water reactor.
  • a spiral circulation channel is provided on the slurry conveying channel of the supercritical water reactor, so that the slurry flow rate is locally increased, and slurry deposition is avoided.
  • a stirrer is arranged in the supercritical water oxidation reactor and extends into the chamber to avoid the deposition of slurry particles in the supercritical water reactor. It not only realizes the complete oxidation of solid particles, but also avoids blockage in the supercritical water oxidation reactor.
  • the supercritical water oxidation reactor may further include an inner liner.
  • the lining can be equivalent to the inner shell of a supercritical water oxidation reactor.
  • the inner liner may be arranged in the chamber, wherein the spiral loop pipe may be wound and arranged along the outer wall of the inner liner.
  • the inner lining can be processed by aluminizing, shot peening and spraying thermal barrier coating.
  • the thermal barrier coating includes multiple aluminum layers and multiple aluminum oxide layers alternately arranged.
  • the inner liner is processed by aluminizing, shot peening and spraying thermal barrier coating.
  • the thermal barrier coating includes multiple aluminum layers and multiple aluminum oxide layers arranged alternately, it is equivalent to An anticorrosive coating is formed on the lining, which can form a dense gel layer on the inner wall of the lining through the high temperature action of the supercritical water to prevent the contact and corrosion of the supercritical water and the lining metal.
  • the key condition for forming a dense gel layer is that there is a dense layer of special metal atoms between the metal and the gel layer.
  • this special metal atom is connected to the bulk metal through a metal bond.
  • the gel layer in the form of a chemical bond.
  • the present invention adopts nickel-based metal.
  • the metal body is aluminized, then the metal surface is forged by shot peening to form a dense metal aluminum atom layer, and then the thermal barrier coating is sprayed through the metal Alternate spraying of aluminum and aluminum oxide ceramic layers, forming 6-8 layers of thermal barrier coatings on the metal surface with a thickness of about 2-3mm. After the thermal barrier coating encounters supercritical water, this thermal barrier coating will transform into a dense gel layer.
  • the gel layer can prevent the supercritical water from contacting and corroding the metal lining.
  • Fig. 4 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure.
  • the supercritical water oxidation reactor 400 includes a shell 401, a heating device 402, a spiral loop pipe 403, a turn-back pipe 404, a stirrer 405, and a cooling device 406.
  • the shell 401 is provided with a slurry inlet 4011, an oxidant inlet 4012, and a material outlet 4013.
  • the spiral loop tube 403 includes one end 4031 of the spiral loop tube and the other end 4032 of the spiral loop tube.
  • the turn-back tube 404 includes an inner tube 4041 with two ends open and an outer tube 4042 with one end open.
  • the agitator 405 includes a rotating shaft 4051.
  • the housing 401, the heating device 402, the spiral loop tube 403, the turn-back tube 404, and the stirrer 405 in the embodiment of the present disclosure may refer to the description of FIGS. 1, 2 and 3 in the present disclosure for the purpose of description For the sake of brevity, I won’t repeat it here.
  • the cooling device 406 is arranged on the side wall to cool the reaction product generated in the chamber; wherein, the heating device 402 and the cooling device 406 can be arranged side by side on the side wall, and the distance between the heating device 402 and the first end wall is less than The distance between the cooling device 406 and the first end wall.
  • the distance between the heating device 402 and the first end wall is smaller than the distance between the cooling device 406 and the first end wall, that is, the heating device 402 is closer to the first end wall, and the cooling device 406 is away from the first end wall. Since the slurry and the oxidant react at a position close to the first end wall, the heating device 402 may be disposed close to the first end wall, and the cooling device 406 may be disposed close to the second end wall.
  • FIG. 5 schematically shows a schematic diagram of a cooling device 406 according to an embodiment of the present disclosure.
  • the cooling device 406 can be composed of cooling sets, covering the outer wall of the supercritical water oxidation reactor 400, each cooling set includes two semi-cooling jackets 4061, the two semi-cooling jackets 4061 can be fixed The holes and bolts 4062 are fixed, and the semi-cooling jacket 4061 can be filled with cooling water. For example, water is filled from one end of the two semi-cooling jackets 4061 according to the arrow in FIG. 5, and then water is discharged from the other end of the two half-cooling jackets 4061.
  • the cooling device 406 when the cooling device 406 cools the reaction product produced in the chamber, it generally does not lower the temperature of the reaction product to normal temperature, but may lower the temperature of the reaction product to higher than normal temperature. , Even higher than the boiling temperature of water, for example, from 500 °C to 300 °C, this design, due to the higher temperature when the reaction product is discharged, not only reduces the burden of cooling the supercritical water reactor, but also increases the supercritical water After the effluent temperature of the oxidation reactor, the temperature of the reaction product itself can be fully utilized to create the necessary conditions for spontaneous evaporation for the subsequent reaction product separation equipment. It should be noted that another function of the cooling device 406 is to prevent the temperature of the chamber from being too high, thereby preventing overheating reactions.
  • a method for processing radioactive organic waste using a supercritical water oxidation reactor is also provided.
  • the supercritical water oxidation reactor required for processing radioactive organic waste may be the supercritical water oxidation reactor described in any one of FIGS. 1 to 4 of the present disclosure.
  • the oxidant and the waste are directly mixed in a supercritical water oxidation reactor, and then the temperature of the oxidant and the waste reaches a certain temperature before the complete reaction occurs.
  • the organic slurry has a large molecular weight and a stable molecular space structure, it is difficult to oxidize in a short time.
  • the waste material imported from the outside will not only lower the temperature of the reaction zone, but also cause a long reaction time of the waste material in the supercritical water oxidation reactor and reduce the reaction efficiency.
  • a spiral loop tube is provided in the chamber of the supercritical water oxidation reactor.
  • the radioactive organic waste flows in the spiral loop tube. It can be fully preheated, heated, and even thermally decomposed, thereby prolonging the pyrolysis time of the radioactive organic waste, ensuring the completeness of the supercritical water oxidation of the radioactive organic waste, and improving the reaction efficiency.
  • Fig. 6 schematically shows a flow chart of using a supercritical water oxidation reactor to treat radioactive organic waste according to an embodiment of the present disclosure.
  • the use of a supercritical water oxidation reactor to process radioactive organic waste includes steps S601 to S604.
  • step S601 the chamber is preheated by the heating device.
  • step S602 when the temperature in the chamber reaches the first temperature, the target solution is introduced into the chamber through the slurry inlet, and the chamber is continued to be heated until the temperature in the chamber reaches the second temperature.
  • an electric heating jacket may be used to preheat the reactor so that the temperature in the reactor chamber reaches the first temperature, which may be 300° C., for example.
  • the target solution may be a sucrose solution
  • the sucrose solution supply pump can be started, the sucrose solution is fed into the chamber through the slurry inlet, and the reactor temperature is heated to a second temperature, where the second temperature is greater than or It is equal to 600°C, for example, it may be 650°C or higher.
  • the oxidant enters the turn-back tube from the oxidant inlet first, and after passing through the inner tube and the outer tube of the turn-back tube in turn, enters the cavity from the opening of the outer tube. room.
  • step S603 the slurry of radioactive organic waste is fed into the spiral loop pipe through the slurry inlet, flows along the pipe of the spiral loop pipe, and flows out from the other end of the spiral loop pipe.
  • the organic waste feed pump is started to remove the radioactive organic
  • the waste slurry is fed into the spiral loop pipe through the slurry inlet.
  • the temperature of the inner shell of the reactor near the nozzle is 650°C ⁇ 800°C, and the temperature of the corresponding outer shell does not exceed 600°C.
  • the temperature of the reaction product is reduced to 120 °C ⁇ 300°C, but not too low, there should be enough temperature to evaporate the reaction product itself.
  • step S604 after the slurry of radioactive organic waste flows out from the other end of the spiral loop pipe, it is mixed with the oxidant entering the chamber from the oxidant inlet and an oxidation reaction occurs.
  • the stirrer is used to stir the oxidation product obtained after the oxidation reaction occurs.
  • the temperature at which the oxidation product is discharged from the discharge port may be between 120°C and 300°C, alternatively, it may be between 150°C and 300°C. between.
  • the general reaction temperature in the related art is 600°C.
  • the reaction temperature of the present disclosure is higher, which effectively improves the reaction rate.
  • the outlet temperature of the oxidation product is high, which can be 300°C, which reduces the burden of the supercritical water reactor.
  • the processing capacity for solid combustibles can reach 20-200kg/h, or even higher.
  • the present disclosure can utilize a supercritical water oxidation reactor to process solid combustible slurry.
  • a supercritical water oxidation reactor By shredding the solid combustibles and directly introducing them into the spiral loop tube, the thermal decomposition in the spiral loop tube can be realized.
  • the supercritical water oxidation reaction After flowing out from the spiral loop tube, the supercritical water oxidation reaction can proceed.
  • the average temperature of supercritical water is 600°C
  • the pyrolysis of organic matter generally takes about 1 second.
  • the residence time of organic matter is at least 8s, and the effect is better than theoretically required.
  • the embodiment of the present disclosure provides a solid material shredder.
  • the solid material shredder includes a guide box, a shredding device, a material box and a colloid mill which are connected to each other and arranged in sequence.
  • the guide box is used to introduce solid materials and make the solid materials fall along the axial direction of the guide box;
  • the shredding device includes a cutter that can rotate under the drive of an external force, and the shredding device is used for cutting
  • the solid material falling along the axial direction of the material box is cut into pieces;
  • the material box is used to drive the movement of the pieces falling from the shredder device through the flowing liquid introduced into the material box;
  • the bottom of the material box is set
  • There is a sieve plate with multiple sieve holes which is used to filter out part of the liquid and fragments smaller than the size of the multiple sieve holes.
  • the colloid mill is set under the sieve plate to filter out the material box. The pieces are ground into a slurry.
  • Figures 7 to 8 schematically show the structure diagram of the solid material shredder according to the first embodiment of the present disclosure.
  • Fig. 7 is a front sectional view of the solid material shredder
  • Fig. 8 is a side view (left or right view) sectional view of the solid material shredder.
  • the solid material shredder 1 of the embodiment of the present disclosure includes a guide box 10, a shredding device 20, a feed box 30 and a colloid mill 40 which are connected to each other and arranged in sequence.
  • the guide box 10 is used to introduce solid materials and make the solid materials fall along the axial direction of the guide box 1 (ie, refer to the vertical direction in FIG. 7).
  • the material guide box may be, for example, a rectangular parallelepiped shaped material guide box.
  • the end of the guide box close to the shredding device 20 in the axial direction may be, for example, an open structure to facilitate solid materials falling into the shredding device.
  • the shredding device 20 includes a cutter that can rotate under the drive of an external force, and the shredding device 20 is used to cut the solid material falling along the axial direction of the guide box 10 into pieces by the cutter.
  • the external force may be, for example, an external force provided by the first motor 2 and/or the second motor 3.
  • the shredding device 20 may include, for example, a cutting assembly 21 for cutting solid materials into blocks.
  • the cutting block assembly 21 includes the above-mentioned cutting knife that can be driven by an external force.
  • the external force is provided by the second motor 3.
  • the shredding device 20 may, for example, further include a pulverizing component 22 for further cutting the blocks cut by the dicing component 21 to obtain fragments.
  • the pulverizing assembly 22 may also include the above-mentioned cutter that can be driven by an external force.
  • the external force is not only provided by the second motor 3, but also provided by the first motor 2. .
  • the second motor 3 is used to drive the cutter included in the cutting assembly 21 to rotate
  • the first motor 2 is used to drive the cutter included in the crushing assembly 22 to rotate.
  • the shredding device 20 may have a housing, for example, and the shredding assembly 21 and the pulverizing assembly 22 are arranged in the housing.
  • the shell can be integrally formed with the guide box 10 and the feed box 30.
  • the material box 30 is specifically used to drive the broken pieces falling from the shredder device 20 to move through the flowing liquid introduced into the material box 30. Furthermore, the bottom of the bin 30 is provided with a sieve plate 31 including a plurality of sieve holes, and the flowing liquid can drive the falling pieces to the area where the sieve plate 31 is located.
  • the blocks can be filtered out of the material box 30 along with part of the liquid, so that the colloid mill 40 can be used for grinding.
  • the mesh size of the sieve plate 31 may be specifically set according to the requirements of the colloid mill 40, for example, the mesh size may be less than 5 mm.
  • at least part of the fragments obtained by shredding by the above-mentioned shredding device 20 should be able to meet the requirement that the width in any direction is less than 5 mm.
  • a shredder material guide hole 50 may be provided between the shredding device 20 and the bin 30 to smoothly introduce the shredded pieces cut by the shredding device 20 into the bin 30.
  • the colloid mill 40 is arranged under the sieve plate 31 provided at the bottom of the material box 30 to grind the fragments of the filtered material box 30. Considering that the liquid flowing in the material box is filtered out with the fragments, the colloid mill 40 does not need to add additional liquid when grinding the fragments.
  • the fragments become slurry under the grinding action of the colloid mill 40, and specifically, for example, can be converted into colloidal particles.
  • the type of the colloid mill 40 can be specifically selected according to actual requirements, so that the particle size of the slurry obtained by grinding can meet the actual requirements. Specifically, the particle size of the slurry obtained by grinding may be less than 50 ⁇ m, for example.
  • the solid material chopper of the embodiment of the present disclosure can directly chop and grind the solid material into a slurry, so the integration is high and the processing efficiency is high.
  • the solid material shredder integrates shredding and grinding functions by setting a shredding device and a colloid mill, when the solid material is radioactive combustible waste, it can effectively reduce radioactive operation links, thereby reducing radioactive pollution .
  • Fig. 9 schematically shows a structural diagram of a shredding device according to an embodiment of the present disclosure.
  • the shredding device 20 of the embodiment of the present disclosure specifically includes a cutting component 21 and a pulverizing component 22.
  • the cutting assembly 21 includes a fixed cylinder 211, a rolling cylinder 212 and a plurality of first cutters 213.
  • the axial direction of the fixed cylinder 211 is perpendicular to the axial direction of the guide box 10, and the axial direction of the fixed cylinder 211 may be, for example, both perpendicular to the vertical direction in FIG. 1 and perpendicular to the guide box 10 Width direction.
  • the fixed cylinder 211 includes a first side wall 2111.
  • the first side wall 2111 is provided with a corresponding first opening 215 and a second opening 216. The two openings are respectively used to communicate with the guide box. 10 and material box 30.
  • the portion of the first side wall 2111 where the first opening 215 is provided can be connected to the side wall of the opening structure of the guide box 10, so that the guide box 10 and the cutting assembly 21 are connected to the first opening 215 via the opening structure. Connected, so that the solid material introduced by the guide box 10 falls into the fixed cylinder 211.
  • the rolling cylinder 212 is arranged in the fixed cylinder 211 along the axial direction of the fixed cylinder 211.
  • the rolling drum 212 includes a second side wall 2121, and the distance between the second side wall 2121 and the first side wall 2111 may specifically correspond to the size of the solid material, so that the solid material falling into the self-guided material box 10 It can fall between the rolling cylinder 212 and the fixed cylinder 211.
  • the plurality of first cutting blades 213 may be specifically arranged on the second side wall 2121 along the circumferential direction of the rolling barrel 212 (that is, the direction surrounding the central axis of the rolling barrel 212). Specifically, the plurality of first cutting blades 213 may be evenly arranged on the second side wall 2121 to form a first blade array.
  • the solid material falls between the rolling cylinder 212 and the fixed cylinder 211 (that is, between the first side wall 2111 and the second side wall 2121), under the cutting action of the first knife array, the solid material can be cut into Lumps.
  • the size of the rolling cylinder 212 and the fixed cylinder 211 can be selected and set according to the size of the solid material, so that the distance between the first side wall 2111 and the second side wall 2121 is not too small. It cannot fall into the solid material, and it will not fall directly along the aperture between the first side wall 2111 and the first blade array without being cut because it is too large.
  • the distance between two adjacent first cutters 213 in the first cutter array can be specifically set according to the cutting requirements, that is, the distance corresponds to the size of the block to be cut.
  • the distance between two adjacent first cutters can be appropriately reduced, and when the solid material needs to be cut into larger sizes, it can be appropriately increased.
  • the distance between two adjacent first cuts may be, for example, on the order of decimeters, for example, 100 mm.
  • the cutting assembly 21 may further include a plurality of third cutters 214, for example.
  • the plurality of third cutting knives 214 may be arranged on the inner surface of the first side wall 2111 along the circumferential direction of the fixed cylinder 211 so as to be opposite to the plurality of first cutting knives 213.
  • the plurality of third cutting knives 214 may be uniformly arranged on the first side wall 2111, for example, to form a second knife array.
  • the aforementioned rolling cylinder 212 can specifically rotate around its central axis under the action of the second external force, so as to fall into the first side wall 2111 and the second side along the axial direction of the guide box 10.
  • the solid material between the walls 2121 can be cut into blocks under the action of the first knife array and the second knife array. Specifically, when the solid material falls between the first side wall 2111 and the second side wall 2121, the solid material is caught between the adjacent first cutting blades 213. With the rotation of the rolling drum 212, the solid material rotates and is continuously cut and refined under the action of the third cutter 214 in the second knife array, thereby being cut into a size smaller than the first side wall 2111 and The distance between the second side walls 2121 is a block.
  • the effective cutting of the solid material is realized, and the size of the block cut into the solid material is limited within a certain range (for example, within the range of 100 mm).
  • the distance between two adjacent third cutters 214 in the second knife array may be equal to or different from the distance between two adjacent first cutters 213, for example.
  • the distance between the two adjacent third cutters 214 may also be on the order of decimeters, for example.
  • the above-mentioned second external force may be provided by the second motor 3 in reference to FIG. 8.
  • the rolling drum 212 rotates slowly under the action of the second external force, and the rotation speed may specifically be 5R/min ⁇ 50R/min.
  • the present disclosure does not limit the rotation speed of the rolling drum 212, and the rotation speed of the rolling drum 212 can be specifically set according to the hardness of the solid material and cutting requirements.
  • the rolling drum 212 may specifically include at least one set of rollers arranged along the axial direction of the fixed drum 211, for example.
  • Each set of rollers includes two opposite rollers, and the side walls of the two opposite rollers are each formed with a first knife array.
  • the two opposed rollers can, for example, be driven by the aforementioned second external force to rotate in opposite directions to bring the solid material falling between the two rollers to the first knife array and Between the second knife array, solid materials are cut.
  • the two opposing rollers can be arranged symmetrically with respect to the central axis of the guide box, and the distance between the two opposing rollers should be smaller than the size of the solid material, so as to avoid along the guide The solid materials falling in the axial direction of the bin directly fall into the crushing assembly 22 or the bin 30 along the distance between two opposite rollers.
  • the above-mentioned crushing assembly 22 can be arranged in the fixed cylinder 211 between the rolling cylinder 212 and the material box 30 to further cut the block obtained by the cutting assembly 21 to obtain a solid Pieces of material.
  • the distance between the crushing assembly 22 and the first side wall 2111 of the fixed cylinder 211 needs to be greater than a preset distance, so that the fragments obtained by the crushing assembly 22 can pass through the first side wall.
  • the space between 2111 and the crushing assembly 22 falls into the bin 30.
  • the preset distance can be specifically set according to the size of the fragments cut by the crushing assembly 22.
  • the preset distance should not be too large, so as to prevent the block obtained by the cutting assembly 22 from directly falling into the bin 30 through the distance between the crushing assembly 22 and the first side wall 2111.
  • the preset distance may be 5 mm, for example.
  • the pulverizing assembly 22 may include, for example, a second cutter for cutting the block into pieces to further reduce the size of the pieces entering the bin 30, which is the size of the colloid mill 40 Grinding provides conditions.
  • the second cutter can be rotated at a high speed under the action of the first external force, to ensure effective cutting of the block.
  • the first external force may be provided by, for example, the first motor 2 shown in FIGS. 7 to 8.
  • the rotation speed of the second cutting knife can be specifically set according to the hardness of the solid material.
  • the rotation speed of the second cutting knife can be 1000R/min-3000R/min.
  • the second cutter of the crushing assembly 22 may specifically include an axial cutter 221 and a radial cutter 222, for example.
  • the axial cutter 221 is arranged along the axial direction of the guide box 10
  • the radial cutter 222 is arranged along a direction perpendicular to the axial direction of the guide box 10 and the axial direction of the fixed cylinder 211.
  • the radial cutter 222 may be coaxial with the axial cutter 221, so that the radial cutter 222 and the axial cutter 221 rotate synchronously around the coaxial central axis under the action of the first external force.
  • the radial cutter 222 may be located between the axial cutter 221 and the material box 30 to further radially cut the block that has been axially cut by the axial cutter 221, so that the resulting fragments
  • the block size is about less than 5mm, ready for the fragments to enter the colloid mill.
  • the shredding device of the embodiment of the present disclosure adopts a shredding method that combines large pieces of material through a slow-rotating roller knife array, and small pieces of material through a high-speed rotating cutter.
  • the size of the obtained fragments is reduced to less than 5mm, and the obtained fragments have good uniformity, so as to prepare for the fragments to enter the colloid mill and be ground into slurry.
  • FIG. 10A to 10B schematically show the structure diagrams of the first cutting knife/third cutting knife according to an embodiment of the present disclosure.
  • 10A is a front view of the first cutting/third cutting knife
  • FIG. 10B is a top view of the first cutting/third cutting knife.
  • the first cutting knife forming the first knife array and/or the second cutting knife forming the second knife array may, for example, adopt a multi-edge knife structure to improve the first knife array and the second knife array.
  • the stability and sharpness of the steel can improve cutting efficiency.
  • the first cutting knife/third cutting knife is a four-sided knife.
  • FIG. 11A to 11B schematically show the structure diagram of the pulverizing component according to an embodiment of the present disclosure.
  • 11A is a front view of the second cutter
  • FIG. 11B is a top view of the second cutter.
  • the above-mentioned pulverizing components 22 may be, for example, a plurality of pulverizing components arranged periodically, and the plurality of pulverizing components 22 are periodically distributed along the central axis of the fixed cylinder 211 in FIG. Blocks falling at different positions in the direction of the central axis of the barrel 211 are cut.
  • Each pulverizing assembly 22 includes a second cutter, and the second cutter has an axial cutter 221 and a radial cutter 222.
  • the number of first motors 2 should be the same as the number of crushing components 22.
  • the axial cutter 221 in the above-mentioned second cutter may be configured as multiple pairs of axial cutters with different heights, and two cutters in each pair of cutters are along the axial direction.
  • the coaxial central axis 223 of the cutter 221 and the radial cutter 222 are symmetrically arranged to perform stepwise cutting of the block. Specifically, the block is first cut by a high-height axial cutter, and then cut by a high-height axial cutter and then dropped, and then cut by a low-height axial cutter, so as to realize the block Cut the object multiple times to facilitate cutting the block into smaller pieces.
  • the above-mentioned radial cutter 222 may be an integrated structure in the radial direction (in a direction perpendicular to the axial direction of the guide box and perpendicular to the axial direction of the fixed cylinder).
  • the two ends of) are cutter structures, which are gradually thinner in the axial direction parallel to the guide box.
  • Fig. 12 schematically shows a structure diagram of a solid material shredder according to a second embodiment of the present disclosure.
  • the solid material shredder 1 of the embodiment of the present disclosure may further include a material receiving box 60 and a gate valve 70, for example.
  • the material receiving box 60 is used for receiving and placing solid materials.
  • the switch of the gate valve 70 is arranged on the outside of the material receiving box 60, and the gate valve 70 is arranged between the material receiving box 60 and the material guide box 10.
  • the gate valve can be switched on and isolated from the material receiving box. Box 60 and guide box 10. Specifically, when solid materials need to be shredded and pulverized, the packaging bag containing the solid materials may be opened and put into the material receiving box 60. At this time, the gate valve 70 is opened, and the solid materials in the packaging bag can be introduced into the guide box 10 from the material receiving box 60.
  • the guide box 10 in the solid material shredder 1 of the embodiment of the present disclosure may, for example, have a pair of opposed third side walls 11, and the pair of third sides Each third side wall 11 in the wall 11 is provided with a plurality of nozzles 111.
  • the nozzles 111 By connecting the nozzles 111 with the pump and the liquid tank, the liquid in the liquid tank can be pumped into the nozzle and sprayed into The guide box 10 is inside.
  • the plurality of nozzles 111 provided on the pair of third side walls 11 may be arranged evenly and symmetrically, so as to introduce liquid evenly and symmetrically at the side walls of the guide box 10, so that the material
  • the solid material introduced in the receiving box 60 can fall along the axial direction of the guide box 10 under the action of the introduced liquid, so that the solid material can fall between the opposite pair of rollers.
  • the flowing liquid in the tank can be the liquid introduced by the nozzle, and the flow of the liquid in the tank can be realized by means of external force to pump the fragments to the area where the sieve plate is located.
  • each third side wall 11 is parallel to the axial direction of the fixed cylinder and the axial direction of the guide box.
  • the entire solid material shredder of the embodiment of the present disclosure is placed in a liquid environment, which can prevent cutting The generation of aerosols in the process of crushing radioactive solid waste, thereby avoiding air pollution.
  • self-feeding can also be realized by means of the liquid introduced by the nozzle without external force, so the equipment size of the entire solid material shredder can be reduced to a certain extent.
  • Fig. 13 schematically shows a structural diagram of a solid material shredder according to a third embodiment of the present disclosure.
  • the solid material shredder 1 of the embodiment of the present disclosure is provided with a diversion pump 80 in order to facilitate the flow of the liquid in the tank 30.
  • a pipe may be provided between the material box 30 and the nozzle 111 of the material guide box 10, for example, so that the liquid in the material box 30 flows into the nozzle 111 through the pipe and is sprayed into the material guide box 10 to achieve Recycling of the liquid in the tank 30.
  • the bin 30 also has larger fragments with a size larger than the mesh size of the sieve plate 31, if this part of the larger fragments is directly discharged, it will pollute the environment.
  • the larger fragments that is, the fragments of the unfiltered material tank 30
  • the box 30 flows into the guide box 10 through the nozzle 111. Therefore, the larger pieces that flow into the guide box 10 can be cut by the shredding device again until the size is smaller than the sieve hole size on the sieve plate 31, and is ground into a slurry by the colloid mill 40.
  • the embodiment of the present disclosure can realize the recovery and reuse of liquid and unground waste through the above-mentioned configuration of the guide pump 80, and thus improve the processing capacity of the solid material shredder.
  • the embodiment of the present disclosure provides a protective equipment and a reaction system of a reaction device.
  • the protective device of the reaction equipment includes a pair of protective end plates and protective components arranged oppositely.
  • the protection component is arranged between a pair of protection end plates, and the protection component includes an outer protection layer, an inner protection layer and a cooling layer.
  • the outer protective layer and a pair of protective end plates enclose a first space.
  • the inner protective layer is arranged in the first space and encloses a pair of protective end plates to form a second space for accommodating the reaction equipment.
  • the inner protective layer is provided with a plurality of diversion holes along the connection direction of the pair of protective end plates, which are used to guide the release of the reaction equipment between the outer protective layer and the inner protective layer.
  • the cooling layer is sandwiched between the inner protective layer and the outer protective layer, and the cooling layer includes a liquid pipeline capable of storing liquid.
  • the protection component is configured as follows: when the reaction device in a working state is accommodated in the second space, liquid is stored in the liquid pipeline, and the first space is a closed space.
  • Fig. 14 schematically shows a schematic structural diagram of the protective device of the reaction equipment according to the first embodiment of the present disclosure.
  • the protective device 1400 of the reaction device 14 of the embodiment of the present disclosure includes a pair of protective end plates 1410 and a protective component 140 that are arranged oppositely.
  • the reaction device 14 is a device whose internal conditions can reach high temperature and pressure, such as a high temperature and high pressure furnace, a reactor, a supercritical water reactor, and the like. It is understandable that the definition standard for high temperature and high pressure herein can be defined according to actual needs, or can be defined by a standard well-known in the industry, which is not limited in the present disclosure.
  • the protection component 140 is arranged between a pair of protection end plates 1410. As shown in FIG. 14, the protection component 140 may specifically include an outer protection layer 141, an inner protection layer 142 and a cooling layer 143.
  • the outer protective layer 141 and the pair of protective end plates 1410 can enclose the first space.
  • the inner protective layer 142 is disposed in the first space, and the inner protective layer 142 and the pair of protective end plates 1410 enclose a second space, and the second space is used to accommodate the reaction device 14.
  • the cooling layer 143 is sandwiched between the inner protective layer 142 and the outer protective layer 141, and the cooling layer includes a liquid pipeline capable of storing liquid.
  • the inner protective layer 142 may be further provided with a plurality of diversion holes along the connection direction of the pair of protective end plates 1410, for example.
  • Each guide hole is formed by a plurality of small holes 1421 opened in the inner protective layer 142 on the side wall close to the reaction device and the side wall close to the outer protective layer.
  • the release material of the reaction device is introduced into the outer protective layer 141 and the inner protective layer 142 through the plurality of flow holes, that is, the released material is introduced into the cooling layer.
  • the outer protective layer 141, the inner protective layer 142, and the cooling layer 143 of the embodiment of the present disclosure may be coaxially arranged.
  • the above-mentioned protective assembly 140 may be specifically configured as; when the reaction device 14 in the working state is accommodated in the second space, the liquid is stored in the liquid pipeline in the cooling layer 143, and the external The first space enclosed by the protective layer 141 and a pair of opposite end plates 1410 is a closed space. Therefore, in this case, when the released material is introduced into the cooling layer, due to the high temperature and high pressure of the released material, and the internal environment of the liquid pipeline is normal temperature and normal pressure or low temperature and normal pressure, the release material will impact the liquid due to the internal and external pressure difference. The pipeline, even the liquid pipeline ruptured.
  • the liquid in the liquid pipeline can cool the release material, and the increase in the space that the release material can fill will reduce the pressure of the release material.
  • the released material after cooling and decompression cannot be released outside the protective device 1400 due to the barrier of the outer protective layer, but can only exist in the first space. Therefore, when the released material is a radioactive gas, it can prevent the released material from polluting the environment And damage to the human body.
  • the above-mentioned liquid pipeline may include a plurality of first pipelines 1431, and the plurality of first pipelines 1431 are connected to a pair of protective end plates 1410. Extending in the connecting direction of, and a plurality of first pipelines are periodically arranged in the direction perpendicular to the inner protective layer 142 and the circumferential direction of the inner protective layer 142.
  • the contact area between the released substance and the liquid pipeline can be increased, thereby improving the cooling efficiency, and through the plurality of first pipelines 1431, more liquid can be stored.
  • the release material impacts and ruptures the first pipeline 1431, the space that the release material can fill is significantly increased, so that the pressure can be quickly relieved and the impact damage of the release material to the outer protective layer 141 can be prevented.
  • the plurality of diversion holes provided on the inner protective layer may be, for example, in the connection direction of the pair of protective end plates 1410 Periodic arrangement, thus further avoiding the concentrated impact of releases on the cooling layer. And therefore, the contact area between the release material and the cooling layer can be increased, and the temperature and pressure reduction efficiency can be further improved.
  • the thickness and material of the inner protective layer and the outer protective layer can be specifically set according to actual conditions.
  • the main body material of the inner protective layer and/or the outer protective layer may include steel.
  • the thickness of the inner protective layer may be, for example, 30 mm to 50 mm, and the material may be, for example, No. 45 steel.
  • the thickness of the outer protective layer can be 30mm-50mm, and its material can be, for example, stainless steel.
  • FIG. 15A schematically shows a structural diagram of a first protective end plate in a pair of protective end plates according to an embodiment of the present disclosure
  • FIG. 15B schematically shows a second protective end of a pair of protective end plates according to an embodiment of the present disclosure Schematic diagram of the board structure.
  • a pair of oppositely disposed protective end plates 1410 may specifically include a first protective end plate 1500 and a second protective end plate 1600.
  • the first protective end plate 1500 and the second protective end plate 1600 may adopt the structures in FIGS. 15A to 15B, respectively.
  • the first protective end plate 1500 of the embodiment of the present disclosure may have a first liquid inlet 1501, a first liquid outlet 1502, and a first liquid passage connecting the first liquid inlet 1501 and the first liquid outlet 1502 1503.
  • the first liquid outlet 1502 is in communication with the liquid pipeline.
  • the first liquid inlet 1501 can be opened or closed under the action of external force.
  • the first liquid inlet 1501 is in an open state when liquid needs to be introduced into the liquid pipeline, and the first liquid inlet 1501 is in an open state when no liquid needs to be introduced.
  • the first protective end plate 1500 can be configured as: when the first liquid inlet 1501 is opened, the liquid introduced from the first liquid inlet 1501 flows through the first liquid passage 1503, and the liquid is self-communicating The first liquid outlet 1502 flows into the liquid pipeline, thereby realizing the introduction of fluid in the liquid pipeline.
  • the first liquid inlet 1501 when liquid is introduced into the first liquid inlet 1501, specifically, for example, it may be connected with a liquid outlet of a liquid storage device (such as a water cooler) to introduce the liquid stored in the liquid storage device.
  • a liquid storage device such as a water cooler
  • the first liquid inlet 1501 can also be in an open state when the liquid needs to be exported, and the first liquid inlet 1501 can also serve as an outlet, as long as it is connected to the suction pump and connected to the inlet of the liquid storage device.
  • the liquid port is connected.
  • the first protective end plate 1500 may be specifically composed of, for example, a first end plate 1510, a second end plate 1520, and a first cylinder 1530.
  • the first cylinder 1530 is located between the first end plate 1510 and the first end plate 1510. Between two end plates 1520. And the size of the first cylinder 1530 matches the first end plate 1510 and the second end plate 1520, or the size of the first cylinder 1530 is smaller than the size of the first end plate 1510 and the second end plate 1520, so as to A first liquid passage 1503 is enclosed between the first end plate 1510 and the second end plate 1520, that is, the hollow portion of the first cylinder 1530 is the first liquid passage 1503.
  • the first liquid inlet 1501 is provided on the first cylinder 1530
  • the first liquid outlet 1502 is provided on the end plate of the first end plate 1510 and the second end plate 1520 which is close to the second protective end plate 1600 .
  • the first liquid outlet 1502 may be disposed on the second end plate 1520.
  • the second end plate 1520 is close to the second protective end plate 1600 relative to the first end plate 1510.
  • the first end plate 1510, the second end plate 1520, and the first cylinder 1530 can be specifically formed by welding or the like to form the first protective end plate 1500, or the first end plate 1510, the second The end plate 1520 and the first cylinder 1530 may also be integrally formed to form the first protective end plate 1500, which is not limited in the present disclosure.
  • the second protective end plate 1600 of the embodiment of the present disclosure may have a second liquid inlet 1601, a second liquid outlet 1602, and a second liquid inlet 1601 that communicates with the second liquid outlet 1602.
  • the second liquid inlet 1601 is in communication with the liquid pipeline.
  • the second liquid outlet 1602 can be opened or closed under the action of an external force.
  • the second protective end plate 1600 can be configured to: when the second liquid outlet 1602 is opened, the liquid in the liquid pipeline flows out of the liquid pipeline from the second cooling liquid inlet 1601 and flows through the second liquid outlet 1602. After the liquid passage 1603 is led out of the second cooling liquid outlet 1602, the storage fluid in the liquid pipeline can be led out.
  • the second liquid outlet 1602 can be specifically connected with the liquid inlet of a liquid storage device (such as a water chiller) when the liquid is discharged, and can be connected to a device such as a motor that can provide suction (such as a pump). Driven by the liquid pump, the liquid stored in the liquid pipeline is led out. It is understandable that the second liquid outlet 1602 can also be in an open state when liquid needs to be introduced, and the second liquid outlet 1602 can also serve as an inlet, as long as the second liquid outlet 1602 is in communication with the liquid outlet of the liquid storage device, And connect the suction pump.
  • a liquid storage device such as a water chiller
  • the second protective end plate 1600 may be specifically composed of a third end plate 1610, a fourth end plate 1620, and a second cylinder 1630, and the second cylinder 1630 is located between the third end plate 1610 and the fourth end plate 1610. Between the end plates 1620. And the size of the second cylinder 1630 matches the third end plate 1610 and the fourth end plate 1620, or the size of the second cylinder 1630 is smaller than the third end plate 1610 and the fourth end plate 1620, so as to A second liquid passage 1603 is enclosed between the third end plate 1610 and the fourth end plate 1620, that is, the hollow portion of the second cylinder 1630 is the second liquid passage 1603.
  • the second liquid outlet 1602 is provided on the second cylinder 1630, and the second liquid inlet 1601 is provided on the end plate of the third end plate 1610 and the fourth end plate 1620 which is close to the first protective end plate 1500 .
  • the second liquid inlet 1601 may be provided on the third end plate 1610.
  • the third end plate 1610 is close to the first protective end plate 1500 relative to the fourth end plate 1620.
  • the third end plate 1610, the fourth end plate 1620, and the second cylinder 1630 may be specifically formed by welding or the like to form the second protective end plate 1600, or the third end plate 1610, the fourth The end plate 1620 and the second cylinder 1630 can also be integrally formed to form the first protective end plate 1600, which is not limited in the present disclosure.
  • the protective device 1400 in order to ensure that the protective device 1400 of the reaction equipment is placed in the protective device 1400, the protective device 1400 should be in a closed state. Therefore, the protective device 1400 can be configured such that when the reaction device in the working state is contained in the second space, the first liquid inlet 1501 and the second liquid outlet 1602 are closed, and the first liquid passage 1503 and the second liquid Liquid is stored in the passage 1603. In this case, by storing liquid in the first liquid passage 1503 and the second liquid passage 1603, it is possible to prevent the incomplete protection due to the impact of the release from the reaction device on the protection end plate. Therefore, the release material released by the reaction device can be completely enclosed in the protective device 1400, so as to prevent the release material from leaking and polluting the environment.
  • the plurality of first pipes 1431 in FIG. 14 may have first and second ends that are oppositely disposed. Then the plurality of first pipelines 1431 can be connected to the two protective end plates to facilitate the introduction and discharge of liquid. Specifically, the first ends of the plurality of first pipelines 1431 are in communication with the first liquid outlet 1502, and the second ends are in communication with the second liquid inlet 1601.
  • the thickness and material of the first end plate 1510, the second end plate 1520, and the first cylinder 1530 in the first protective end plate 1500 can be specifically set according to actual requirements.
  • the thickness of the first end plate 1510, the second end plate 1520 and/or the side wall of the first cylinder 1530 may be, for example, 30 mm to 70 mm.
  • the main material of the first end plate 1510, the second end plate 1520 and/or the first cylinder 1530 can be steel, for example, stainless steel, 45 steel, or the like.
  • the thickness and material of the third end plate 1610, the fourth end plate 1620, and the second cylinder 1630 in the second protective end plate 1600 can be specifically set according to actual requirements.
  • the thickness of the third end plate 1610, the fourth end plate 1620, and/or the side wall of the second cylinder 1630 may be 30 mm to 70 mm, for example.
  • the main material of the third end plate 1610, the fourth end plate 1620 and/or the second cylinder 1630 may be steel, for example, stainless steel, 45 steel, or the like.
  • FIG. 16 schematically shows a structural diagram of the protective device of the reaction equipment according to the second embodiment of the present disclosure
  • FIG. 17A schematically shows a front sectional view of the protective device of the reaction equipment with reference to FIG. 16
  • FIG. 17B schematically shows The side sectional view of the protective device of the reaction equipment in reference to FIG. 16 is shown.
  • the difference between the protective device 1400 of the reaction device 14 in the embodiment of the present disclosure and the protective device in FIG. 14 is that the liquid pipeline of the cooling layer 143 except for the multiple first pipelines 1431, A plurality of second pipelines 1432 may also be included.
  • the plurality of second pipelines 1432 are extended in the circumferential direction of the inner protective layer 142, and the plurality of second pipelines 1432 are connected in the connecting direction of a pair of protective end plates and perpendicular to the inner protective layer.
  • the direction of the protective layer is periodically arranged. Specifically, as the distance between the multiple second pipelines and the inner protective layer increases, the size of the second pipelines 1432 periodically arranged in the direction perpendicular to the inner protective layer also gradually increases.
  • the specific size of the plurality of second pipelines 1432 may be determined according to the distance between the two first pipelines of the plurality of pairs of first pipelines 1431 arranged opposite to the inner protective layer. So that each of the plurality of second pipelines 1432 can communicate with a group of first pipelines 1431 at an equal distance from the first inner protective layer through a pipeline connector, so that the plurality of second pipelines 1432 The pipeline 1432 and the plurality of first pipelines 1431 communicate with each other to form a cage structure.
  • the protective device of the reaction device of the embodiment of the present disclosure may be configured to:
  • the liquid introduced by 1501 flows into the first liquid passage 1503, the first pipe 1431, and the second pipe 1432 in sequence. Therefore, when the liquid is introduced, the liquid can flow into the first pipe 1431 and the second pipe 1432, so as to ensure that both the first pipe 1431 and the second pipe 1432 can store liquid.
  • the gap between the released object and the liquid pipeline can be effectively increased.
  • the contact area, and therefore the release material can achieve rapid temperature and pressure reduction, the release material will instantly cool down to liquid water, which will completely dissolve it.
  • the protective device 1400 will not be damaged, so that the released objects can be well confined inside the outer protective layer 141. Effectively avoid environmental pollution.
  • reaction equipment may be a high-temperature and high-pressure equipment, for example, a supercritical water reaction equipment, a high-temperature and high-pressure furnace, or a reactor.
  • the protective device of the reaction equipment may be any one of the protective devices described in reference to FIGS. 14-17B.
  • the protective device specifically includes a pair of protective end plates and protective components.
  • the protective component includes an outer protective layer, an inner protective layer and a cooling layer, and the cooling layer is sandwiched between the outer protective layer and the inner protective layer.
  • the reaction equipment can be placed in the second space enclosed by the inner protective layer of the protective device and a pair of protective end plates. I won't repeat them here.
  • the reaction system since the reaction system not only has reaction equipment, but also includes a protective device for the reaction equipment, it can effectively prevent the reaction equipment from exploding due to an accident, the high-temperature and high-pressure releases on the external environment Unforeseen accidents caused by the impact of According to an embodiment of the present disclosure, the above-mentioned reaction device may specifically be a supercritical water reaction device.
  • the present disclosure provides a supercritical water oxidation system and method.
  • the critical water oxidation system and method can convert solid combustibles into inorganic substances through supercritical water oxidation, and at the same time recover radioactive metal elements in organic substances, thereby achieving the purpose of minimizing waste.
  • the processing capacity of using the supercritical water oxidation system and method to treat radioactive solid combustible waste can reach at least 20kg/h ⁇ 200kg/h, reaching the scale of engineering application.
  • Fiber fabrics working clothes, absorbent paper, gloves,
  • the volume reduction ratio of gas jackets, etc. can reach 100-150
  • the volume reduction ratio of plastics and rubber can reach 60-90
  • the volume reduction ratio of waste resin can reach 30-90
  • the volume reduction ratio of waste wood can reach 80-120.
  • the supercritical water oxidation system includes a water supply device for providing water and a target solution; an oxidizer supply device for providing an oxidizer for the supercritical water oxidation reaction; and a solid combustible material cutting and grinding machine for Grinding solid combustibles to a slurry; supercritical water oxidation reactor for receiving slurry, oxidant, water and target solution obtained after grinding solid combustibles, and providing a reaction zone for supercritical water oxidation reaction; separation; Equipment for separating the effluent from the supercritical water oxidation reactor.
  • Fig. 18 schematically shows a schematic diagram of a supercritical water oxidation system according to an embodiment of the present disclosure.
  • the supercritical water oxidation system shown in FIG. 18 is only an example of the supercritical water oxidation system to which the embodiments of the present disclosure can be applied to help those skilled in the art understand the technical content of the present disclosure, but it cannot be used as the supercritical water oxidation system of the embodiments of the present disclosure.
  • the water oxidation system is improperly defined.
  • the supercritical water oxidation system includes a water supply device 181, an oxidant supply device 182, a solid combustibles chopper and refiner 183, a supercritical water oxidation reactor 184, and a separation device 185.
  • the water supply device 181 is used to supply water and a target solution.
  • the water supply device 181 may include a plurality of containers for respectively containing water and a target solution.
  • the target solution may be a sucrose solution
  • the sucrose solution supply pump can be activated to draw the sucrose solution from the container.
  • the water supply device 181 may also include a high-pressure pump for transferring water and the target solution to the supercritical water oxidation reactor 184.
  • the oxidant supply device 182 is used to provide an oxidant for the supercritical water oxidation reaction.
  • the type of oxidant is not limited.
  • it can be liquid oxygen, hydrogen peroxide and so on.
  • the oxidant supply device 182 is connected to the supercritical water oxidation reactor 184, and the oxidant can be input into the supercritical water oxidation reactor 184 to realize the supercritical water oxidation reaction.
  • the oxidant supply device 182 may include a Dewar 1821, a water bath vaporizer 1822 and a high-pressure oxygen cylinder 1823.
  • Liquid oxygen can be fed from the Dewar 1821 to the water bath vaporizer 1822 through a low temperature and high pressure liquid oxygen pump, and then enter the high pressure oxygen cylinder group 1823 from the water bath vaporizer 1822.
  • the one-way valve can be opened, and oxygen from the high-pressure oxygen cylinder group 1823 is input into the supercritical water oxidation reactor 184.
  • the material of the liquid oxygen equipment, pipes, valves, and components may be ultra-cold low-temperature steel.
  • the solid combustibles chopping and refining machine 183 is used to grind the solid combustibles to a slurry.
  • the solid combustibles may be stored in a packing box 186, from which the solid combustibles are input into the solid combustibles chopping refiner 183.
  • the solid combustibles can first enter the large roller array for shredding, then enter the small rotary cutter for shredding, and finally pass Control the speed of the roller, the speed of the rotary cutter, and the water volume of the diversion pump to carry out the crushing and colloidal grinding and grinding, so as to realize the cutting and grinding of the radioactive solid waste.
  • the solid combustibles chopping and refining machine 183 can grind the solid combustibles to a certain particle size range, for example, the solid combustibles can be pulverized to below 50 ⁇ m.
  • the one-way valve can be opened, and the slurry is fed from the solid combustibles chopping and refining machine 183 to the supercritical water oxidation reactor 184.
  • the material of the solid combustibles shredding refiner 183 may be stainless steel.
  • the supercritical water oxidation reactor 184 is used to receive slurry, oxidant, water and target solution obtained by grinding solid combustibles, and to provide a reaction zone for supercritical water oxidation reaction.
  • the supercritical water oxidation reactor 184 can be charged with excess oxidant to ensure that the slurry is fully oxidized.
  • the reaction temperature of the supercritical water oxidation reactor 184 can be Between 600°C and 800°C, the pressure can be between 20Mpa and 30Mpa. After the slurry is fully oxidized in the supercritical water oxidation reactor 184, an oxidation product can be obtained, which is transported to the separation device 185 through the discharge port.
  • the separation device 185 is used to separate the effluent of the supercritical water oxidation reactor 184.
  • the separation device 185 may include an activated carbon filter column 1851 and a high efficiency filter 1852, which are disposed at the exhaust port of the separation device 185.
  • a volatile organic compound online monitor 1853 is provided at the exhaust port of the separation device 185.
  • the evaporation tank of the separation device 185 is equipped with a level gauge (not shown in FIG. 18).
  • the water outlet of the separation device 185 is equipped with an online chemical oxygen demand monitor 1854.
  • the evaporation tank of the separation device 185 is equipped with a pH meter 1855.
  • the COD value of the discharged liquid substance is monitored by the online chemical oxygen demand monitor 1854 provided on the separation device 185; and/or the COD value of the discharged liquid substance is monitored by the separation device 185
  • the volatile organic compound online monitor 1853 is set up to monitor the VOC value of the discharged gaseous substances; and/or the pH value of the solution in the evaporation tank in the separation device is monitored by the pH meter 1855 set on the separation device 185; and/or the pH value of the solution in the evaporation tank in the separation device is monitored by the separation device
  • the thermometer installed on the 185 monitors the temperature of the solution in the evaporation tank in the separation equipment and/or the temperature in the cooling barrel.
  • the separation device 185 further includes a back pressure valve 1856, wherein one end of the back pressure valve 1856 is connected to a casing pipe (not shown in FIG. 18) through a pipe, and the other end of the back pressure valve is used to communicate with the overpressure valve through the pipe.
  • the discharge port of the critical water oxidation reactor 184 is connected.
  • the water supply device 181, the oxidant supply device 182, the solid combustibles chopping and refining machine 183, the supercritical water oxidation reactor 184 and the separation equipment 185 are small in size, large in capacity, and can realize remote automatic For control, each part can be a skid-mounted independent unit to facilitate the on-site combination of the overall equipment.
  • high temperature and high pressure equipment and liquid oxygen cryogenic equipment can be designed with safety protection measures such as explosion-proof isolation chamber and explosion venting channel.
  • FIG. 19 schematically shows a flowchart of a method for treating solid combustibles by using a supercritical water oxidation system according to an embodiment of the present disclosure.
  • a supercritical water oxidation system may be used to treat solid combustibles, as shown in FIG. 19, and the specific method may include steps S1901 to S1906.
  • step S1901 the temperature of the chamber of the supercritical water oxidation reactor is increased to the first temperature.
  • an electric heating device may be used to preheat the reactor so that the temperature in the reactor chamber reaches the first temperature, for example, 300°C.
  • step S1902 the oxidant is fed into the chamber through the oxidant supply device.
  • step S1903 the target solution is fed into the chamber through the water supply device, and the chamber is continuously heated until the temperature in the chamber reaches the second temperature.
  • the target solution may be a sucrose solution.
  • the water supply device may start a sucrose solution supply pump, and input the sucrose solution into the chamber through the slurry inlet of the supercritical water oxidation reactor, and heat the reactor to a temperature
  • the second temperature wherein the second temperature is greater than or equal to 600°C, for example, may be 650°C or higher.
  • step S1904 the solid combustibles are pulverized into a slurry by a solid combustibles chopping and grinder, and the slurry is fed into the chamber, so that the slurry and the oxidant undergo oxidation reaction to obtain an effluent.
  • multiple steps in steps S1901 to S1904 may be performed simultaneously. For example, first start the electric heating device of the supercritical water oxidation reactor, and start the water supply pump in the water supply device at the same time, the water supply device is filled with water, and the pump flow rate is adjusted to a low state.
  • the supercritical water oxidation reactor is heated until the temperature reaches 300°C, then the sucrose peristaltic pump and the oxidant feeding device are started, and the supercritical water oxidation reactor is heated with concentrated sucrose solution until the temperature reaches 600°C or more.
  • the oxidation temperature of supercritical water is maintained at 650°C to 750°C, and the pressure is maintained at 20-25MPa.
  • the solid combustibles chopping and refining machine can grind the solid combustibles to slurry in advance, and then input the slurry into the chamber when the slurry needs to be processed.
  • step S1905 the effluent is sent to the separation device through the discharge port of the supercritical water oxidation reactor.
  • the organic matter when the supercritical water oxidation reactor is shut down, the organic matter can be stopped first, and oxygen supply can be continued, so as to oxidize the residual organic matter in the equipment. Then, oxygen intake is stopped and the water supply is continued until the water temperature drops to 300. After °C, stop the water supply pump, slowly open the outlet back pressure valve, so that the remaining liquid inside the supercritical water oxidation reactor is slowly released to the separation equipment.
  • step S1906 the effluent is separated by a separation device.
  • the separation device 185 can separate the effluent of the supercritical water oxidation reactor 184 into salt residue, distilled water and purified gas.
  • the solid combustibles are radioactive solid combustibles, they can be oxidized into salt solution and gas, and can be separated into radioactive salt residue, distilled water and purified gas through the separation device 185.
  • the radioactive salt residue can be discharged after a period of time.
  • Most of the distilled water can be recycled into the solid combustibles chopper and refiner 183 for recycling. A small amount of distilled water can be collected or discharged directly, and the purified gas can be collected or discharged directly.
  • the supercritical water oxidation system of the present disclosure may be used to process solid combustible slurry.
  • solids if solids are directly fed into the supercritical water oxidation reactor, it will cause blockage in the supercritical water oxidation reactor.
  • This disclosure breaks through the technical bottleneck that the feed is liquid or gas at home and abroad, and the solids can be shredded and refined. After that, the particles of the slurry are lower than 50 ⁇ m, and the slurry is pumped into the supercritical water oxidation reactor, which eliminates obstacles to prevent large particles from depositing inside the supercritical water reactor.
  • the oxidant and the waste are directly mixed in a supercritical water oxidation reactor, and then the temperature of the oxidant and the waste reaches a certain temperature before the complete reaction occurs.
  • the organic slurry has a large molecular weight and a stable molecular space structure, it is difficult to oxidize in a short time.
  • the oxidant when the temperature in the chamber of the supercritical water oxidation reactor reaches a certain temperature, the oxidant is filled, so that the temperature of the oxidant can be increased in advance, and then the slurry is fed into the chamber of the supercritical water oxidation reactor, The slurry can be fully and timely thermally decomposed, the completeness of the supercritical water oxidation of the organic slurry is ensured, and the reaction efficiency is improved.
  • the method for treating solid combustibles using the supercritical water oxidation system includes cutting and grinding of solid combustibles, supercritical water oxidation, and effluent self-evaporation separation and purification. Not only is the process flow short, but also Solid combustibles do not require pyrolysis pretreatment, and at the same time, solid organics are directly oxidized by supercritical water. Further, the present disclosure can be higher than the supercritical water reaction temperature in the related art, and the reaction temperature can reach 600° C. or more, which effectively improves the reaction rate.
  • Fig. 20 schematically shows a schematic diagram of a supercritical water oxidation reactor according to an embodiment of the present disclosure.
  • the supercritical water oxidation reactor 2000 includes a first shell 2001, a heating device 2002 and a spiral loop pipe 2003.
  • a chamber for providing the reaction zone is formed inside the first shell 2001, and at least a slurry inlet 2011, an oxidant inlet 2012, and a material outlet 2013 are provided on the first shell 2001.
  • the first housing 2001 may include an outer shell and an inner shell (for example, the inner shell may be the inner liner 2014 in FIG. 20), and the shape, material, and size of the outer shell and the inner shell are not limited.
  • the main body of the first housing 2001 may be cylindrical, the inner diameter of the outer shell is 80-219 mm, and the length is 1000-9000 mm; the inner diameter of the inner shell is 40-133 mm, and the length is 1000-9000 mm.
  • the heating device 2002 is used to increase the temperature of the chamber.
  • the type of the heating device 2002 is not limited.
  • the heating device 2002 may be a heating jacket.
  • the heating jacket can be sleeved on the outer wall of the housing 2001, and heat is transferred to the cavity inside the housing 2001 through heat conduction.
  • the present disclosure does not limit other heating methods.
  • the two ends of the outer shell of the supercritical water oxidation reactor 2000 can be equipped with pressure gauges, the two ends and the middle of the inner shell can be equipped with temperature probes, and the heating jacket and the outer wall of the outer shell can be equipped with temperature probes.
  • the heating device 2002 may cover a part of the outer wall of the first housing 2001.
  • the heating device 2002 may be arranged on the outer wall corresponding to the predetermined area where the outlet of the spiral loop pipe 2003 flows out of the slurry, so as to cover a part of the first housing 2001.
  • the heating device 2002 includes four heating jackets, covering the middle of the first housing 2001 to the area from the spiral loop pipe 2003 to the outlet of the slurry.
  • the spiral loop tube 2003 is arranged in the chamber, and one end 2031 of the spiral loop tube is in communication with the slurry inlet 2011, wherein the spiral loop tube 2003 is set so that the slurry is introduced from the slurry inlet 2011 into the spiral loop tube 2003, along the spiral loop tube 2003
  • the pipe flows, and flows out of 2032 from the other end of the spiral loop pipe, and mixes with the oxidant flowing into the chamber from the oxidant inlet 2012, and an oxidation reaction occurs.
  • the spiral circulation pipe 2003 can flow the organic slurry along the circulation pipe. On the one hand, it increases the degree of flow of the organic slurry and on the other hand increases the flow velocity of the organic slurry, which can increase the heat of the organic slurry. Solution efficiency.
  • the spiral circulation tube 2003 may be disposed close to the inner wall of the housing 2001.
  • the spiral circulation pipe 2003 may be disposed between the outer housing and the inner housing.
  • the spiral circulation pipe 2003 can be wound around the inner shell for installation.
  • the supercritical water oxidation reactor 2000 of the present disclosure may be used to process solid combustible slurry.
  • thermal decomposition in the spiral loop tube 2003 can be realized.
  • the supercritical water oxidation reaction can be carried out.
  • the average temperature of supercritical water is 600°C
  • the pyrolysis of organic matter generally takes about 1 second.
  • the residence time of organic matter is at least 8s or more, and the effect is better than theoretically required.
  • the organic matter if the organic matter is directly fed, the organic matter will cool the temperature of the reaction zone and reduce the reaction effect.
  • the reaction temperature is 600°C
  • the pyrolysis time of the organic matter is about 1s
  • the reaction temperature is 550°C
  • the time required for the pyrolysis of the organic matter is 5min, which will reduce the reaction efficiency. It can be seen that, compared with the prior art, the present disclosure has a very fast response time and improves processing efficiency.
  • FIG. 21 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure.
  • the supercritical water oxidation reactor 2100 includes a first shell 2101, a heating device 2102, a spiral loop tube 2103 and a turn-back tube 2104.
  • the first shell 2101 is provided with a slurry inlet 2111, an oxidant inlet 2112, and a discharge port 2113.
  • the spiral loop tube 2103 includes one end 2131 of the spiral loop tube and the other end 2132 of the spiral loop tube.
  • first housing 2101, the heating device 2102, and the spiral loop tube 2103 in the embodiments of the present disclosure can refer to the description of FIG. 20 in the present disclosure.
  • details are not repeated here.
  • the turn-back tube 2104 is disposed in the chamber.
  • the turn-back tube 2104 includes an inner tube 2141 with two ends open and an outer tube 2142 with one end open.
  • the outer tube 2142 is sleeved outside the inner tube 2141, and the inner tube 2141 Connect with the oxidant inlet 2112.
  • the oxidant after the oxidant is introduced from the oxidant inlet 2112, it passes through the inner tube 2141, then enters the outer tube 2142, and is finally discharged from an opening at one end of the outer tube 2142.
  • the turn-back tube 2104 may be disposed at the central axis position of the chamber.
  • the shape, material, and size of the inner tube 2141 and the outer tube 2142 are not limited.
  • the diameter of the inner tube 2141 can be ⁇ 25 ⁇ 42mm
  • the wall thickness can be 4-6mm
  • the diameter of the outer pipe can be 42mm or more
  • the wall thickness can be 4-6mm
  • the length can be between 3000mm and 6000mm.
  • the size of the turn-back tube 2104 is moderate, which can effectively reduce the production cost and is beneficial to market applications.
  • the turning-back tube can make the oxidant in the tube rise as much as possible, increasing the preheating time.
  • the turn-back tube is set at the central axis of the supercritical water reactor, so that the heating temperature can reach the highest.
  • the supercritical water oxidation reactor further includes a stirrer and an inner liner.
  • the agitator includes a rotating shaft, and the rotating shaft extends through the first shell into the cavity, and/or the rotating shaft extends through the discharge port into the cavity.
  • the inner liner is arranged in the chamber, and the spiral circulation pipe is wound around the outer wall of the inner liner.
  • the lining can be equivalent to the inner shell of a supercritical water oxidation reactor.
  • the inner liner may be processed by aluminizing, shot peening, and spraying thermal barrier coating.
  • the thermal barrier coating includes multiple aluminum layers and multiple aluminum oxide layers alternately arranged.
  • the inner liner is processed by aluminizing, shot peening and spraying thermal barrier coating.
  • the thermal barrier coating includes multiple aluminum layers and multiple aluminum oxide layers arranged alternately, it is equivalent to An anticorrosive coating is formed on the lining, which can form a dense gel layer on the inner wall of the lining through the high temperature action of the supercritical water to prevent the contact and corrosion of the supercritical water and the lining metal.
  • the key condition for forming a dense gel layer is that there is a dense layer of special metal atoms between the metal and the gel layer.
  • this special metal atom is connected to the bulk metal through a metal bond.
  • the gel layer in the form of a chemical bond.
  • the present invention adopts nickel-based metal.
  • the metal body is aluminized, then the metal surface is forged by shot peening to form a dense metal aluminum atom layer, and then the thermal barrier coating is sprayed through the metal Alternate spraying of aluminum and aluminum oxide ceramic layers, forming 6-8 layers of thermal barrier coatings on the metal surface with a thickness of about 2-3mm. After the thermal barrier coating encounters supercritical water, this thermal barrier coating will transform into a dense gel layer.
  • the gel layer can prevent the supercritical water from contacting and corroding the metal lining.
  • the supercritical water oxidation reactor further includes a cooling device arranged on the side wall for cooling the reaction product generated in the chamber; wherein the heating device and the cooling device may be arranged side by side on the side wall, In addition, the distance between the heating device and the first end wall is smaller than the distance between the cooling device and the first end wall.
  • Fig. 22 schematically shows a schematic diagram of a supercritical water oxidation reactor according to another embodiment of the present disclosure.
  • the supercritical water oxidation reactor 2200 includes a first shell 2201, a heating device 2202, a spiral loop tube 2203, a turn-back tube 2204, a stirrer 2205, and a cooling device 2206.
  • the first shell 2201 is provided with a slurry inlet 2211, an oxidant inlet 2212, and a discharge port 2213.
  • the spiral loop tube 2203 includes one end 2231 of the spiral loop tube and the other end 2232 of the spiral loop tube.
  • the turn-back tube 2204 includes an inner tube 2241 with two ends open and an outer tube 2242 with one end open.
  • the agitator 2205 includes a rotating shaft 2251. According to the embodiment of the present disclosure, the positions of the slurry inlet 2211, the oxidant inlet 2212, and the discharge port 2213 are not limited.
  • housing 2201, the heating device 2202, the spiral loop tube 2203, the turn-back tube 2204, etc. in the embodiment of the present disclosure may refer to the description of FIG. 20 and FIG. 21 in the present disclosure. For the sake of brevity of description, it is not here. Repeat it again.
  • the agitator 2205 includes a rotating shaft 2251, the rotating shaft 2251 passes through the housing 2201 and extends into the chamber, and/or the rotating shaft 2251 passes through the discharge port 2213 to extend into the chamber.
  • the agitator 2205 may also include a rotor, a spacer sleeve, a magnetic block and other components required by the agitator (not shown in FIG. 22).
  • the first housing 2201 includes a first end wall, a side wall, and a second end wall opposite to the first end wall.
  • the slurry inlet 2211 is provided on the side wall
  • the oxidant inlet 2212 is provided on the side wall.
  • the agitator 2205 and the discharge port 2213 are provided on the second end wall.
  • the discharge port 2213 may also be provided on the side wall.
  • the stirrer 2205 may be a magnetic stirrer.
  • the supercritical water oxidation reactor 2200 When the supercritical water oxidation reactor 2200 is installed vertically, it can be installed at the bottom of the supercritical water oxidation reactor 2200, mainly for Stir the sediment at the bottom of the reactor to prevent solid particles from depositing, compacting, and blocking the discharge port.
  • the distance between the heating device 2202 and the first end wall is smaller than the distance between the cooling device 2206 and the first end wall, that is, the heating device 2202 is closer to the first end wall, and the cooling device 2206 is away from the first end wall. Since the slurry and the oxidant react at a position close to the first end wall, the heating device 2202 can be installed close to the first end wall, and the cooling device 2206 can be installed close to the second end wall.
  • FIG. 23 schematically shows a schematic diagram of a cooling device 506 according to an embodiment of the present disclosure.
  • the cooling device 2206 can be composed of cooling sets, covering the outer wall of the supercritical water oxidation reactor 2200.
  • Each cooling set includes two semi-cooling jackets 2261.
  • the two semi-cooling jackets 2261 can be fixed
  • the holes and bolts 2262 are fixed, and the half-cooling jacket 2261 can be filled with cooling water.
  • the water is discharged from the other end of the two half-cooling jackets 2261.
  • the cooling device 2206 when the cooling device 2206 cools the reaction product produced in the chamber, it generally does not lower the temperature of the reaction product to normal temperature, but may lower the temperature of the reaction product to higher than normal temperature. , Even higher than the temperature at which water boils, for example, from 500°C to 300°C.
  • This design not only reduces the burden of cooling the supercritical water reactor when the reaction product is discharged, but also increases the temperature of the effluent from the supercritical water oxidation reactor, which can make full use of the temperature of the reaction product itself for the subsequent reaction Product separation equipment creates the necessary conditions for spontaneous evaporation.
  • another function of the cooling device 2206 is to prevent the temperature of the chamber from being too high, thereby preventing overheating reactions.
  • Fig. 24 schematically shows a schematic diagram of a separation device according to an embodiment of the present disclosure.
  • the separation device 2400 includes an evaporation tank 2401 and a cooling inner tub 2402.
  • the evaporation tank 2401 is used to receive the effluent from the supercritical water oxidation reactor, where the effluent is a multi-phase mixture, and the evaporation tank 2401 is provided with a first cooling coil 2411 and a slag discharge port 2412, and a first cooling plate
  • the pipe 2411 is used to stabilize the temperature of the solution in the evaporation tank 2401 within the target temperature range after the multi-phase mixture flows into the evaporation tank 2401, and the slag discharge port 2412 is used to discharge solid substances in the multi-phase mixture.
  • the cooling inner barrel 2402 includes a second cooling coil 2421 and a condensing pool 2422.
  • the second cooling coil 2421 is used to cool the vapor evaporated in the evaporation pool 2401
  • the condensing pool 2422 is used to receive the second cooling coil 2421 to cool the steam.
  • the condensing pool 2422 is provided with a drain 2423 for discharging liquid substances.
  • the wall of the cooling inner barrel 2402 is provided with a plurality of holes for the vapor evaporated in the evaporation pool 2401 to enter the cooling inner barrel 2402.
  • the evaporation pool 2401 and the cooling inner barrel 2402 are enclosed in the second shell, the evaporation pool 2401 is arranged under the cooling inner barrel 2402, and the top of the second shell is provided with an exhaust port 2403 for discharging gaseous substances in the multi-phase mixture. .
  • the types of the first cooling coil 2411 and the second cooling coil 2421 are not limited.
  • it may be a spiral cooling pipe.
  • the arrangement of the first cooling coil 2411 and the second cooling coil 2421 is not limited, as long as the corresponding functions can be realized.
  • the solid-liquid-gas polymorphic substances are separated in the integrated machine, eliminating the need for cooling equipment, gas-liquid separation equipment, and liquid cooling.
  • Equipment and gas cooling equipment simplify the processing flow.
  • the evaporation tank 2401 can receive the effluent of the supercritical water reactor, and the effluent can be a multi-phase mixture.
  • the evaporation tank 2401 can evaporate and concentrate the effluent, and then recover the solid matter, and the steam rises to cool In the inner barrel 2402.
  • the effluent of the supercritical water reactor may be a high temperature and high pressure fluid, for example, the temperature of the reacted effluent itself is 150-300°C and the pressure is 25 MPa.
  • a cooling coil is provided in the evaporation pool 2401 so that the effluent can always be in a boiling state. That is, the first cooling coil 2411 stabilizes the temperature of the solution in the evaporation tank 2401 within the target temperature range, for example, it may be around 100° C., so that the solution can boil stably in the evaporation tank 2401.
  • the evaporated steam can rise into the cooling inner barrel 2402, and the radioactive metal elements contained in the reaction effluent can flow out from the slag outlet 2412 in the form of inorganic salts and be recovered.
  • the condensate pool 2422 is provided with a sleeve for receiving the multi-phase mixture of the condensate pool 2422 in the evaporation pool, and the tube wall of the condensate pool 2422 is provided with multiple small holes, and the condensate pool 7022 is a multi-phase mixture. A plurality of small holes are scattered and discharged into the condensation pool 2422 evaporation pool through the condensation pool 2422.
  • a volatile organic compound online monitor 2404 is provided at the exhaust port 2403 of the separation device 2400.
  • a chemical oxygen demand online monitor 2405 is provided at the drain 2423 of the separation device 2400.
  • the evaporation tank 2401 of the separation device 2400 is equipped with a pH meter 2406.
  • the multi-phase mixture may include two or more substances among solid substances, liquid substances, and gaseous substances.
  • the multi-phase mixture contains both solid matter and gaseous matter, or contains solid matter, liquid matter and gaseous matter at the same time.
  • the multi-phase mixture may be a mixture obtained after the organic solvent distillation residue is treated by supercritical water oxidation technology, for example, may be obtained after the organic solvent distillation residue is treated by a supercritical water oxidation reactor
  • the effluent, generally supercritical water oxidation liquid effluent is salty wastewater, or radioactive wastewater, or inorganic brine.
  • a separation device is used to process the multi-phase mixture, so that the solid matter in the multi-phase mixture is evaporated and concentrated at the bottom of the evaporation tank, for example, separated in the form of inorganic salt residue; so that the liquid in the multi-phase mixture
  • the substance evaporates in the evaporation tank and is cooled by the cooling inner barrel, and can be discharged from the drain of the condensing pool; so that the gaseous substance in the multi-phase mixture can be directly discharged from the top of the separation equipment.
  • the separation of the multi-phase mixture can be realized at the same time, the processing flow is not only short, but also the one-time investment of the equipment and the equipment operating cost are effectively reduced, and the maximum volume reduction of the multi-phase mixture is realized.
  • Fig. 25 schematically shows a schematic diagram of a cooling inner tub according to an embodiment of the present disclosure.
  • the wall of the cooling inner barrel 2501 is provided with a plurality of holes 2511 for the vapor evaporated in the evaporation pool to enter the cooling inner barrel 2501.
  • cooling inner barrel 2501 in the embodiment of the present disclosure can refer to the description of FIG. 24 in the present disclosure, and for the sake of brevity of description, it will not be repeated here.
  • the second cooling coil 2512 in the cooling inner tub 2501 can be filled with cooling water, so that the temperature in the cooling inner tub 2501 is lower than the temperature in the evaporation pool, and the second cooling coil 2512 is filled with water After that, the temperature of the steam can be lowered.
  • water vapor, oxygen, and carbon dioxide evaporated in the evaporation tank can enter the cooling inner barrel 2501 from a plurality of holes 2511 provided on the barrel wall, in the upward flow direction shown by the arrow in FIG. 25. After the steam meets the cold air, it condenses to form water droplets and falls into the condensing pool 2513, and then is discharged from the drain 2514. The oxygen and carbon dioxide can be exhausted from the exhaust port 2515 at the top.
  • the volume of the condensing pool 2513 is not limited.
  • the volume of the condensing pool 2513 can be 50L to 500L, and the condensing pool 2513 can be connected to the external annular pipe through multiple radiant pipes, and the water conduction capacity can be 800kg/h to 8000kg/h.
  • the cooling coil 2512 may be a horizontally wound spiral cooling tube, and the size is not limited.
  • a plurality of holes 2511 are left on the wall of the barrel for gas to pass through.
  • the condensation inner barrel 2501 can condense water vapor at 100°C into water at 60°C to 90°C, and the condensing capacity can be 200kg/h to 2000kg/h. h.
  • the volume of the cooling coil area is not limited. For example, the volume can be 1000L. Most of the condensed water is returned to the water supply tank of the supercritical water oxidation reactor for reuse, and a small amount can be discharged.
  • Fig. 26 schematically shows a schematic diagram of a sleeve according to an embodiment of the present disclosure.
  • evaporation tank 2601 in the embodiment of the present disclosure may refer to the description of FIGS. 24 to 25 in the present disclosure, and for the sake of brevity of description, details are not repeated here.
  • the evaporation tank 2601 is provided with a sleeve 2611 for receiving the polymorphic phase mixture.
  • a plurality of small holes 2612 are distributed on the wall of the sleeve 2611, and the polymorphic phase mixture is dispersed and discharged through the plurality of small holes 2612. Into the evaporation pond 2601.
  • the size of the sleeve 2611 is not limited.
  • the diameter of the sleeve 2611 can be ⁇ 42 ⁇ 50mm, and the wall thickness can be 4 ⁇ 6mm.
  • the size of the small hole 2612 is not limited.
  • the diameter of the small hole can be 2 to 3 mm, and its function is mainly to dissolve and disperse the high-speed fluid through the small hole 2612 on the outlet pipe.
  • the type of the sleeve 2611 is not limited.
  • the sleeve 2611 may be a straight tube or a spiral tube.
  • the separation device may further include a back pressure valve 2613.
  • One end of the back pressure valve 2613 is connected to the sleeve 2611 through a pipe, and the other end of the back pressure valve 2613 is used to connect to the discharge port of the supercritical water oxidation reactor through the pipe.
  • the effluent from the supercritical water oxidation reactor flows through the back pressure valve through the pipeline. After the back pressure valve is opened, the effluent can spiral around the evaporation tank when passing through the evaporation tank through the sleeve. The heat is transferred to the water at 100°C. After that, it can be passed through the cooling inner barrel through a pipe and connected with the back pressure valve, and then returned to the evaporation tank after decompression, where the gas-water mixture is sprayed into the evaporation tank (100°C, normal pressure).
  • the oxidation product first enters the evaporation tank after being discharged from the discharge port of the supercritical water oxidation reactor, where the oxidation product relies on its own temperature to achieve the purpose of evaporation.
  • the effluent can be divided into three parts: radioactive metal salt residue, distilled water, and purified gas.
  • the radioactive elements in the effluent are intermittently discharged as salt slag in the form of metal salts.
  • the steam vaporized from the evaporation tank is cooled above the evaporation tank and recycled in the form of distilled water.
  • the oxygen and carbon dioxide in the effluent are It is purified after being washed by the evaporation pool and steam condensed water.
  • the decontamination factor can reach 10 5.
  • the cesium in the water vapor is less than one hundred thousandth of the concentration of cesium in the evaporation tank.
  • the decontamination factor can reach 10 9 , so the steam can be deeply purified.
  • the effluent temperature of the supercritical water oxidation reactor is much higher than the traditional effluent temperature.
  • the effluent of the supercritical water oxidation reactor that is, when the oxidation product is discharged from the discharge port, the temperature when the oxidation product is discharged from the discharge port can be between 150°C and 300°C, while the temperature of the traditional effluent is generally It is 100°C.
  • the separation device of the present disclosure is used to separate the oxidation product, the temperature of the oxidation product discharged from the supercritical water reactor can be made higher, and the burden of cooling the supercritical water reactor is reduced. After increasing the temperature of the effluent from the supercritical water oxidation reactor, the necessary conditions for spontaneous evaporation are created for the subsequent effluent separation equipment.
  • the embodiment of the present disclosure provides a supercritical water oxidation system.
  • the system includes a reactor, a protection device, a reactor, an oxidant supply device and an organic material supply device.
  • the reactor includes a reactor shell, the reactor shell is provided with an oxidant feed port, an organic material feed port, and a feed port, and the reactor discharges reaction products through the feed port.
  • the protective device includes an outer protective layer, a cooling layer and an inner protective layer, wherein the inner protective layer and the outer protective layer enclose a first space and a second space.
  • the cooling layer includes a liquid pipeline capable of storing liquid, the liquid pipeline is arranged in the first space, the reactor is arranged in the second space, and the discharge port of the reactor extends to the first space except the area where the liquid pipeline is located Area, so that the reaction product discharged from the discharge port can be cooled by the liquid stored in the liquid pipeline.
  • the oxidant supply device is communicated with the oxidant feed port, and the organic matter feed device is communicated with the organic matter feed port.
  • FIG. 27 schematically shows a schematic structural diagram of a supercritical water oxidation system according to an embodiment of the present disclosure
  • FIG. 28 schematically shows a cross-sectional view of A-A in FIG. 27.
  • the supercritical water oxidation system 2700 of the embodiment of the present disclosure includes a reactor 500, a protective device 600, an oxidant supply device 700, and an organic material supply device 800.
  • the oxidant supply device 700 and the organic material supply device 800 are respectively used to provide the oxidant and organic matter to the reactor 500.
  • the reactor 500 includes a reactor shell 510, and the reactor shell is provided with an organic material feed port 501, an oxidant feed port 502, and a feed port 503.
  • the reactor 500 may specifically be a supercritical water reactor or even an ultra-supercritical water reactor.
  • supercritical refers to a state where the temperature exceeds 374°C and the pressure exceeds 22Mpa.
  • Ultra-supercritical refers to the supercritical temperature above 700°C.
  • the solubility of inorganic salts in organic matter is zero.
  • organic matter specifically, for example, radioactive organic matter
  • the separation of organic matter is realized by using the feature of inorganic salt with zero solubility above 550°C.
  • the above-mentioned reactor 500 may specifically discharge the reaction product obtained after separation through a discharge port.
  • the protective device 600 includes an outer protective layer 610, an inner protective layer 620, and a cooling layer 630.
  • the cooling layer 630 includes a liquid pipeline 631 capable of storing liquid, and the inner protective layer 620 and the outer protective layer 610 enclose a first space 272 and a second space 273.
  • the liquid pipe 631 is arranged in the first space 272, and the reactor 500 is arranged in the second space 273.
  • the discharge port 503 of the reactor 500 extends to the area of the first space 272 except the area where the liquid pipe 631 is located, so that the reaction product discharged from the discharge port 503 can be stored in the liquid pipe 631
  • the liquid cools down.
  • the discharge port 503 may specifically extend to the bottom space in the first space 272, wherein, in actual use, the reactor 500 and the protective device 600 in FIG. 27 should be placed vertically, and organic matter enters.
  • the inlet 501 is at the bottom.
  • the oxidant supply device 700 is connected to the oxidant feed port 502 to provide the oxidant to the space (reaction chamber) surrounded by the reactor shell 510.
  • the organic material supply device 800 is connected to the organic material feed port 501 to provide organic material to the reaction chamber surrounded by the reactor shell 510.
  • the above-mentioned supercritical water oxidation system 2700 can effectively cool the reaction product ejected from the discharge port 503 through the liquid stored in the liquid pipeline 631 of the protection device 600, and thus obtain residue, condensate and exhaust gas. Therefore, the above system 2700 has an all-in-one machine that integrates the functions of supercritical reaction and reaction product cooling and separation.
  • an additional separator which is beneficial to the promotion of supercritical water oxidation technology. application.
  • FIG. 29 schematically shows the structure diagram of the inner protective layer in reference to FIG. 27.
  • the outer protective layer 610 includes an outer sleeve 611 and a pair of side wall end plates 612 oppositely arranged.
  • the liquid pipeline 631 may specifically include a plurality of double-layer sleeves.
  • the multiple double-layer sleeves are specifically extended in the connection direction of the pair of side wall end plates 612, and the multiple double-layer sleeves are arranged in the radial direction of the outer sleeve 611 and the outer sleeve. 611 is periodically arranged in the circumferential direction.
  • Each of the plurality of double-layer casings includes an outer casing 6311 and an inner casing 6312.
  • the inner diameter of the outer sleeve 611 may be, for example, The length can be 3000-6000mm, and the material can be steel (for example, 304 stainless steel), the ambient pressure is normal pressure, and the temperature is 100°C. There are two main functions, one is to receive the reaction product discharged from the discharge port 503, and the other is to serve as the second protective barrier of the reactor.
  • the outer casing size in the above double casing can be
  • the inner casing size can be The pressure that the inner pipe can withstand is, for example, 3 MPa to 5 MPa, and the temperature that can withstand is 600°C.
  • the inner protective layer 620 includes a coaxial first cylinder 621 and a pair of opposite second cylinders 622.
  • the first cylinder 621 is disposed between the pair of second cylinders 622 and is connected to the The second cylinder 622 is coaxial.
  • the first cylinder 621 includes a first cylinder side wall 6211, and the first cylinder 621 is a structure with open ends.
  • each of the pair of second cylinders 622 includes a first end plate 6221 and a second cylinder side wall 6222.
  • the first end plate 6221 is an annular plate structure whose inner ring size matches the size of the first cylinder 621, and the pair of second cylinders 622 are fixedly connected to the first cylinder 621 via the first end plate 6221.
  • the first cylinder side wall 6211, the first end plate 6221, and the outer sleeve 611 enclose the first space 272
  • the first cylinder 621, the second cylinder 622 and a pair of side wall end plates 612 enclose Into the second space.
  • a plurality of first ports are provided on the above-mentioned first end plate 6221 for communicating with the outer sleeves 6311 of the plurality of double sleeves respectively.
  • the second cylinder side wall 6222 of each of the pair of second cylinders 622 has a first opening 6222A, and one of the first openings serves as a first inlet. Liquid port, the other first opening serves as the first liquid outlet.
  • the protective device can be configured such that when the reactor set in the second space is in working condition, the liquid is cyclically introduced from the first liquid inlet and flows through multiple double-layer sleeves. After the outer sleeve 6311 of the tube, it is led out from the first liquid outlet to cool the reaction product discharged from the outlet 503.
  • each of the pair of second cylinders 622 further includes a second end plate 6223 opposite to the first end plate 6221, and a second end plate 6223 disposed on the first end plate.
  • the length of the inner casing of each double casing of the above-mentioned multiple double casings is greater than that of the outer casing, and a plurality of second interfaces 6224A may be provided on the dividing plate 6224, Yu is respectively connected with the inner casing 6312 of the multiple double casings.
  • the above-mentioned first opening 6222A may be specifically arranged on the second cylindrical side wall 6222 between the first end plate 6221 and the boundary plate 6224. Since the first opening is a liquid inlet or a liquid outlet, through the above arrangement, the liquid introduced into the first liquid inlet can only flow into the outer sleeve 6311 and not into the inner sleeve 6312.
  • the second end plate 6223 may be provided with a plurality of communication holes 6223A, for example, for connecting the inner sleeve 6312 with the second space 273 where the reactor 500 is located.
  • the outer sleeve 6311 has two functions when the liquid is passed into it. One is to cool the reaction product discharged from the discharge port 503, and the other is to cool the discharge introduced by the inner sleeve under abnormal conditions.
  • the inner sleeve 6312 and the outer sleeve 6311 are independent and not connected spaces, and the inner sleeve 6312 is isolated from the outer space of the protective device 600 by the outer sleeve forming the space 273, it can be effectively Avoid accidental releases from spraying out of the external space.
  • the protective device 600 of the embodiment of the present disclosure can cool down normal reaction products and abnormal releases. On the basis of realizing the product separation function, it also has protective functions, and therefore can effectively avoid Various hazards caused by abnormal high-temperature and high-pressure releases ejected from the external space.
  • the second end plate 6223 and the boundary plate 6224 may be, for example, an annular plate structure having the same size as the first end plate 6221.
  • the side walls and end plates of the first cylinder and the second cylinder can be defined by the inner diameter It is composed of thick walls, the working pressure is 3MPa ⁇ 5MPa, and the temperature is 600°C.
  • the thick wall can be composed of an outer skin and a main material, the outer skin can be made of 304 stainless steel, and the main material can be made of No. 45 carbon steel.
  • the cooling layer 630 may include, for example, a condensate collecting tray 632 and a plurality of gas pipelines 633 in addition to the above-mentioned multiple double-layer sleeves.
  • the condensate collecting tray 632 is disposed between two adjacent sets of double-layer sleeves periodically arranged in the radial direction of the outer sleeve in the first space 272.
  • each group of double-layer casings includes a plurality of double-layer casings located in the same radial direction.
  • the condensate collection tray 632 may be located near the discharge port 503 in reference to FIG. 28, and the outer protective layer 610 is also provided with a drain port 6112, which is connected to the condensate collection tray. 632 is connected.
  • the condensate collecting tray 632 has a closed structure on the first surface close to the discharge port 503, and has an open structure on the second surface far away from the discharge port 503.
  • the condensate collecting tray 632 has a plurality of grooves 6321 periodically arranged in the axial direction of the outer sleeve 611. The plurality of grooves 6321 extend in a direction perpendicular to the connecting direction of the first disk surface and the second disk surface.
  • the above-mentioned multiple gas pipes 633 extend along the connecting direction of the first disk surface and the second disk surface at the multiple grooves 6321, and the multiple gas pipes 633 have an open structure at the first end close to the first disk surface, and The second end close to the second disk surface is a closed structure, and the second ends of the multiple gas pipes 633 are higher than the second disk surface, and the multiple gas pipes 633 have multiple jets on the sidewalls higher than the second disk surface. So that the mixture of steam and non-condensable gas in the reaction product discharged from the discharge port can be transmitted through the plurality of gas pipelines 633, and sprayed from the gas injection port to the second surface of the condensate collecting tray 632 away from the discharge port 503 side.
  • the steam sprayed to the side of the second disk surface away from the discharge port 503 acts as the liquid stored in the outer sleeve 6311 to reduce the temperature to form condensate, fall into the condensate collecting tray 632, and exit the protective device through the drain port 6112 600.
  • the outer sleeve 611 of the outer protective layer 610 may further be provided with an exhaust port 6111 on the second surface of the condensate collecting tray 632, which is away from the discharge port 503, so as to In the non-condensable gas discharge protection device 600. And/or, the outer sleeve 611 of the outer protective layer 610 may also be provided with a slag discharge port 6113 on the wall of the barrel close to the discharge port 503, so that the salt slag in the reaction product discharged from the discharge port 503 is affected by gravity. Down discharge the protective device 600.
  • part of the steam in the reaction product discharged from the discharge port 503 may have cooled and become condensate before evaporating to the gas pipeline. Therefore, when the salt slag is discharged from the slag discharge port 6113, there will be some The condensate is discharged.
  • the supercritical water oxidation system may also be provided with a VOC (volatile organic compound) online monitor at the location of the exhaust port 6111, and a COD (chemical Oxygen demand) online detector, and set a pH online monitor at the location of the slag discharge port 6113, so as to determine whether the reaction product will harm the environment.
  • VOC volatile organic compound
  • COD chemical Oxygen demand
  • the embodiments of the present disclosure can effectively realize the separation of reaction products through the arrangement of the above-mentioned gas pipeline and the condensate collecting tray, so that the volume reduction of organic matter can be achieved to the greatest extent.
  • FIG. 30 schematically shows a front cross-sectional view of the reactor of an embodiment of the present disclosure
  • FIG. 31 schematically shows an enlarged view of the structure of the dashed frame area in reference to FIG. 30, and
  • FIG. 32A schematically shows the reference diagram The BB cross-sectional left view in 31, and
  • FIG. 32B schematically shows a right side view with reference to the BB cross-sectional view in FIG. 31.
  • the reactor housing 510 included in the reactor 500 of the embodiment of the present disclosure may include a first end wall 511, a housing side wall 512, and a second end wall 513 disposed opposite to the first end wall.
  • the oxidant feed port 502 is provided on the first end wall 511
  • the discharge port 503 is provided on the second end wall
  • the organic material feed port 501 is provided on the side wall 512 of the housing close to the second end wall 513.
  • the material used for the reactor shell 510 may be INCONEL 625, for example, the inner diameter of the shell side wall 512 is about 80-219 mm, and the length is about 1000-6000 mm.
  • the reactor 500 may further include, for example, a plurality of organic substance conveying pipes 520.
  • the plurality of organic substance conveying pipes 520 are connected along the first end wall 511 and the second end wall 513.
  • the line direction extends in the reactor shell 510, and the plurality of organic substance conveying pipes 520 includes a first end and a second end opposite to the first end.
  • the organic substance conveying pipe 520 close to the organic substance inlet 501 has a first end. One end is in communication with the organic feed port 501.
  • the plurality of organic substance conveying pipes may be arranged at equal intervals in the direction around the central axis of the reactor 500, and the organic substance conveying pipes may be, for example, 12, 6, 4, etc.
  • the present disclosure does not limit the number of the organic matter conveying pipes.
  • the reactor 500 may also include an end loop 530, which is arranged in the reactor shell 510 near the first end wall 511, and the end loop 530 530 communicates with the second ends of the plurality of organic substance conveying pipes 520, so that the organic substance flowing in from the first end of the organic substance conveying pipe can flow into the end loop 530.
  • the end loop 530 is provided with a plurality of first discharge holes 531 on the side wall close to the second end wall 513, and/or, a plurality of organic substance conveying pipes 520 are located close to the central axis of the reactor 500 and close to A plurality of second discharge holes 521 are provided on the side wall of the first end wall 511, and the transferred organic matter can be evenly sprayed into the reactor 500 through the first discharge hole 531 and/or the second discharge hole 521
  • the center of the area near the first end wall 511 (specifically may be a central chamber).
  • the reactor 500 may further include a third cylinder 540 and a feeding plate 550.
  • the third cylinder 540 is sleeved on the outside of the plurality of organic substance conveying pipes 520 and the end ring pipe 530.
  • the third cylinder 540 includes a third end plate 541 and a third cylinder side wall 542.
  • the third end plate 541 has a first feed hole 5411 corresponding to the oxidant feed port 502.
  • the feeding plate 550 is disposed between the third end plate 541 and the end ring pipe 530.
  • An oxidant transmission channel 8 is formed between the feeding plate 550 and the third cylinder 540, and a plurality of second feeding holes 551 are provided on the feeding plate 550.
  • the internal space of the reactor 500 can be divided into two regions as shown in FIG. 30 according to the setting region of the second discharge hole 521.
  • the first area 51 is the area close to the oxidizer feed port 502. In this area, the oxidizer and organic matter can be sprayed uniformly through the arrangement of the above-mentioned discharge hole and the feed hole. A supercritical oxidation reaction occurs in one zone.
  • the second area 52 is the area close to the organic material inlet 501. Since the organic material and oxidant are not sprayed into this area, and because the second area 52 is close to the outlet 503, the reaction product obtained by the reaction in the first area 51 is It can be transported to the second zone 52 and discharged from the reactor 500 through the discharge port 503.
  • the reactor 500 of the embodiment of the present disclosure through the arrangement of the organic substance delivery pipe 520, the end loop 530, the third cylinder 540, and the feed plate 550, can make the oxidant and organic matter can pass from the reactor 500.
  • the ends and sides of the sprayer are evenly sprayed into the center of the first area 51. Therefore, the oxidant and the organic matter can be fully contacted and mixed to fully react, and therefore the center temperature of the first zone of the reactor can be promoted to reach 700-800°C, ensuring that the advantages of the supercritical water oxidation reaction are fully utilized.
  • the reactor 500 may further include an inner liner 560 and a loop sleeve 570, for example.
  • the inner liner 560 is arranged between the shell side wall 512 and the third cylinder side wall 542, and the circulation sleeve 570 is spirally wound on the shell side wall 512 along the inner liner 560 between the inner liner 560 and the shell side wall 512 .
  • a second liquid inlet 5121 and a second liquid outlet 5122 are also provided on the side wall 512 of the housing.
  • the circulation sleeve 570 includes a third end and a fourth end opposite to each other. The third end is in communication with the second liquid inlet 5121, and the fourth end is in communication with the second liquid outlet 5122.
  • the second liquid inlet 5121 is close to the second end wall 513, and the second liquid outlet 5122 is close to the first end wall 511.
  • the heat of the reaction product transferred in the second region 52 can be transferred to the circulation close to the first end wall 511.
  • the sleeve 570 realizes the heating of the injected oxidant and organic matter, thereby further increasing the reaction temperature of the organic matter and the oxidant, and ensuring the full utilization of the advantages of the supercritical water oxidation reaction.
  • the above-mentioned inner liner 560 and the circulating sleeve 570 may be GH4169, for example, the inner diameter of the inner liner 560 may be 40-133 mm, and the length may be 1000-6000 mm.
  • the spiral outer diameter of the circulation sleeve 570 can be close to the inner diameter of the side wall 512 of the casing, for example, the pitch is 50mm, and the pitch is filled with stainless steel mesh (for example, 800 mesh stainless steel mesh), thereby further increasing the heat conduction area and liquid of the inner liner 560
  • the residence time is to ensure sufficient absorption of the heat in the second zone 52 and sufficient heating of the organic matter and the oxidant injected from the side. Therefore, the temperature of the reaction product transferred to the discharge port 503 is not too high, and the reaction temperature of the organic matter and the oxidant can reach the ultra-supercritical condition.
  • the above-mentioned reactor 500 can also A heating assembly 580 is included.
  • the heating component 580 is arranged outside the first zone 51 and is used to increase the temperature in the reactor shell, and thus heat the oxidant and organic matter to be transferred.
  • the heating element 580 may be used to preheat the reactor, for example, the reactor may be preheated to 300°C.
  • the above-mentioned reactor 500 may further include a cooling assembly 590.
  • the cooling component 590 is arranged outside the second area 52 and is used to cool the reaction product of the organic matter and the oxidant. Then, the reaction product of the organic matter and the oxidant undergoes the dual cooling of the circulation jacket 570 and the cooling assembly 590, so that the temperature of the reaction product can be effectively reduced, for example, it can be reduced to 120°C to 300°C. It is understandable that the temperature of the reaction product discharged through the discharge port 503 should not be too low, and a sufficient temperature should be ensured so that the water in the reaction product can evaporate in the form of steam.
  • the above-mentioned reactor 500 may also include agitating Components 5100.
  • the stirring assembly 5100 includes a rotating shaft that passes through the reactor shell and the discharge port and extends into the second area. By rotating the rotating shaft, the reactants can be stirred and the discharge port 503 can be prevented from being blocked.
  • the stirring assembly 5100 may be a magnetic stirrer adopting the standard force stirring technology of the reactor, for example, it may be a magnetic stirrer of model CY-2, which is not limited in the present disclosure.
  • FIG. 33 schematically shows a structural diagram of an organic material supply device according to an embodiment of the present disclosure.
  • the organic material supply device 800 of the embodiment of the present disclosure may include a first device 810 and a second device 820.
  • the first device 810 includes an organic material supply assembly 811, a lye tank 812, a first peristaltic pump 813, a first high pressure pump 814, and a first one-way valve 815.
  • the first peristaltic pump 813 is in communication with the lye tank 812
  • the first high-pressure pump 814 is respectively in communication with the lye tank 812 and the first peristaltic pump 813
  • the first one-way valve 815 is arranged at the first high-pressure pump 814 and the organic material feed port Between 501.
  • the first device 810 is used to provide organic matter that needs to react with the oxidant.
  • the reason why the lye is added to the organic matter is that the organic matter slurry and the lye liquor are mixed in a certain proportion (the lye liquor accounts for 30% to 100% of the weight of the organic matter) and then transported to the organic matter conveying pipe, which can make the organic matter and the lye
  • the organic matter is deeply pyrolyzed into small molecules and then sprayed into the first region 51 from the discharge hole to achieve rapid oxidation of the organic matter and oxidant while releasing a large amount of heat. It is ensured that the center temperature of the first region 51 can meet the requirements of ultra-supercritical.
  • the alkaline hydrolysis of organic matter is an endothermic reaction
  • the alkaline hydrolysis of organic matter can absorb heat in the outer space of the first area, thereby effectively reducing the temperature of the area near the reactor shell 510 and reducing the reaction
  • the requirements for high temperature resistance of the shell material of the device since the alkaline hydrolysis of organic matter is an endothermic reaction, when transported in the organic matter conveying pipe, the alkaline hydrolysis of organic matter can absorb heat in the outer space of the first area, thereby effectively reducing the temperature of the area near the reactor shell 510 and reducing the reaction The requirements for high temperature resistance of the shell material of the device.
  • the second device 820 includes a sucrose solution tank 821, a water tank 822, a second peristaltic pump 823, a second high pressure pump 824 and a second one-way valve 825.
  • the second peristaltic pump 823 is connected to the sucrose solution tank 821
  • the second high-pressure pump 824 is connected to the water tank 822 and the second peristaltic pump 823, respectively
  • the second one-way valve 825 is provided at the second high-pressure pump 824 and the organic feed port 501 between.
  • the reactor 500 can be preheated by referring to the heating assembly 580 in FIG. 30, and after the preheating to 300°C, the second device 820
  • the sucrose solution is connected to the organic feed port 501, and the sucrose solution is introduced into the organic conveying pipe 520. Since the reactor 500 is preheated to 300°C, the sucrose solution will generate a lot of heat due to pyrolysis in the 300°C environment, which can affect the reactor Further heating.
  • the first device 810 is connected to the organic material feed port 501, the organic material to be oxidized is introduced into the organic material delivery pipe 520, and the oxidant is introduced through the oxidant feed port 502, and the first
  • the organic matter in the area 51 and the oxidant instantly undergo a supercritical water oxidation reaction under an environment of 650°C, releasing a large amount of heat, so that the temperature in the central area of the first area 51 reaches 700-800°C and reaches the ultra-supercritical condition, then the organic matter injected subsequently That is, the supercritical water oxidation reaction can occur with the oxidant, so that the organic matter is completely pyrolyzed and gasified, and the advantages of the supercritical water oxidation reaction can be fully utilized.
  • the above-mentioned organic material supply component 811 can specifically select different components according to the type of organic material that needs to be oxidized.
  • the organic material is an organic waste liquid
  • only the liquid tank needs to be used as the organic material supply component 811.
  • the organic matter is a solid organic matter
  • a device capable of cutting and grinding the solid organic matter into a slurry should be used as the organic matter supply component 811.
  • the above-mentioned oxidant supply device 700 may include, for example, a liquid oxygen dewar, a liquid oxygen pump, a one-way valve, a liquid oxygen vaporizer, and a high-pressure oxygen cylinder group to provide the reactor 500 with oxidant.
  • the above-mentioned supercritical water oxidation system may further include, for example, a monitoring component, which includes at least one of the following: arranged on the reactor shell 510, at the outlet 503, and a condensate collection tray 632
  • the setting of the monitoring component can be used to control the pressure and/or flow rate of the oxide feed, the pressure and/or flow rate of the organic feed, and the temperature and pressure of the reactor 500.
  • FIG. 34 schematically shows a structural diagram of a rotary cutting refiner in an embodiment of the present disclosure
  • FIG. 35 schematically shows a top view of the rotary cutting refiner in reference to FIG. 34.
  • the rotary cutter refiner 811 shown in FIG. 34 to FIG. 35 can be used as the organic matter supply component to cut and grind the solid organic matter into a slurry.
  • the rotary cutting refiner 811 includes a guide box 8111, a shear knife, and a colloid mill 8114 that are connected to each other and arranged in sequence.
  • the guide box 8111 is used to introduce solid organic matter and liquid (the liquid here may be, for example, the condensate flowing out of the condensate collection tray 632 in FIG. 28 to realize the recovery and utilization of the liquid), the guide box 8111 There is a diversion hole at the bottom of the.
  • the shearing knife is arranged above the diversion hole at the bottom of the guide box 8111, and is used to cut the falling solid organic matter into 1 ⁇ 5mm slag.
  • the colloid mill 8114 is used to grind the slag flowing out of the guide hole into a slurry.
  • the shearing knife and the colloid mill are coaxial to rotate synchronously under the action of external force.
  • the above-mentioned shearing blade includes a primary shearing blade 8112 and a secondary shearing blade 8113.
  • the primary shearing blade 8112 is used to cut solid organic matter into pieces of 10-50 mm, and the secondary shearing
  • the knife 8113 is used to cut the fragments into the slag of 1 to 5 mm, and the secondary shearing knife 8113 is arranged under the primary shearing knife 8112.
  • the primary shearing knife 8112 is mainly composed of a primary rotary cutting knife 8112A, a primary stationary upper knife 8112B, and a primary stationary lower knife 8112C.
  • there are 4 first-level stationary upper cutters 8112B which are evenly fixed on the inner wall of the guide box 8111, and the position is about the lower third of the guide box 8111.
  • the first-stage stationary upper cutter 8112B is triangular with a triangular center. It is about 190mm from the side wall of the guide box 8111.
  • the first-stage stationary lower cutter 8112C is located directly below the first-stage stationary upper cutter 8112B, and the distance between the two just accommodates the first-stage rotary cutter 8112A.
  • the first-stage stationary lower cutter 8112C is also triangular, and the distance from the triangular center to the side wall of the guide box 8111 is about 250mm.
  • the main body of the first-level rotary cutter 8112A is a narrow strip-shaped plate with a length of about 570mm, a width of about 100mm, and a thickness of about 5mm.
  • Two upward blades are welded on both sides of the shaft center.
  • the blade height is about 50mm away from the shaft center. Approximately 100mm, all blades are sharpened with sharp corners.
  • the purpose of setting the primary rotary cutter 8112A is to shear radioactive solid waste at high speed in the vertical and horizontal directions.
  • the secondary shearing knife 8113 is composed of a secondary rotary cutter 8113A and a secondary stationary plate 8113B, and the secondary rotary cutter 8113A is a narrow and long strip plate, The length is about 570mm, the width is about 100mm, and the thickness is about 5mm.
  • the distance between the secondary stationary plate 8113B and the secondary rotary cutter 8113A is as small as possible, and the secondary stationary plate 8113B is uniformly distributed in diameter When the broken pieces pass through the hole, they are cut again by the secondary rotary cutter 8113A.
  • the slag obtained by the secondary shearing knife 8113 flows into the colloid mill 8114 through the diversion hole under the barrel, and is further ground to 50 ⁇ m in the colloid mill 8114.
  • the temperature of the supercritical water reaction of organic matter can reach 700°C to 800°C, which solves the inadequate treatment of difficult waste (such as amines, anion exchange resins, etc.)
  • difficult waste such as amines, anion exchange resins, etc.
  • the supercritical water oxidation system of the present disclosure integrates the functions of organic matter oxidation, effluent separation, and equipment protection, which brings great convenience to engineering applications.
  • the processing capacity of the supercritical water oxidation system of the embodiments of the present disclosure can reach 20-200 kg/h, which can meet the volume reduction of solid combustibles produced by uranium ore purification, nuclear fuel pretreatment plants, nuclear fuel manufacturing plants, spent fuel reprocessing plants, etc. Harm reduction needs.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Food Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

一种超临界水氧化反应器（100），包括：壳体（101），内部形成用于提供反应区的腔室，壳体（101）上至少设置有浆料入口（1011）、氧化剂入口（1012）和出料口（1013）；加热装置（102），用于提高腔室的温度；螺旋环流管（103），设置在腔室内，螺旋环流管（103）的一端与浆料入口（1011）连通，其中，浆料从浆料入口（1011）导入螺旋环流管（103）之后，沿螺旋环流管（103）的管道流动，并从螺旋环流管（103）的另一端流出；浆料从螺旋环流管（103）的另一端流出之后，与从氧化剂入口（1012）流入腔室的氧化剂混合并发生氧化反应。还提供了一种利用超临界水氧化反应器处理放射性有机废物的方法，一种反应设备的防护装置及反应***，以及一种超临界水氧化***和采用其处理固体可燃物的方法。

Description

超临界水氧化处理放射性有机固体废物 技术领域
本发明涉及固体废物处理领域，具体是涉及一种超临界水氧化***和固体废物处理方法。
背景技术
随着原子能工业发展和放射性同位素日趋广泛的应用，放射性废物日趋增多。如不经处理或处理不当而外排，会使环境遭受放射性污染。不仅影响动植物的生长，恶化水体，且危害人体健康，甚至对后代产生不良影响。
超临界水氧化法是一种新型的湿法氧化技术。通过利用有机废物、水、氧气在超临界水体系中完全混溶的特点，将有机物氧化分解为水、二氧化碳、氮气等气体，所含放射性核素转变为无机盐，从而完成对有机溶剂蒸残液的处理。一般地，超临界水是指温度超过374℃、压力超过22Mpa的一种特殊状态的水。在超临界水状态下有机废物和氧气在超临界水体系中完全混溶，当超临界水温度超过550℃，无机盐在其中的溶解度为零。利用超临界水的这种性能，可以将有机物转化为二氧化碳、水和无机盐，利用无机盐在550℃以上溶解度为零的特点实现放射性元素的分离。
由于水是一种常见的溶剂，各种污染物本身一般都含有水。超临界水氧化技术可以应用于环保、化工、煤气化、核电和火电、新材料合成等多种领域中，用于处理污水、污泥等污染物。
目前，美、法、俄、日等国相关核研究单位近年来积极开展有机废物超临界水处理技术研究，建立了实验装置，部分工作已达到中试规模。研究认为，超临界水氧化法分解效率高、处理周期短、无明火、二次废物少、环境友好，适合处理多种有机废物，是一种极具潜力的处理技术。
但是发明人在实现本公开构思的过程中，发现现有技术中至少存在如下问题：
在相关技术中，超临界水氧化反应器的处理过程一般是在反应器内将氧化剂和废料直接进行混合，然后待氧化剂和废料的温度达到一定温度之后才能完全发生反应。在这种情况下，废料不仅会降低反应区的温度，而且导致废料在超临界水氧化反应器中的反应时间长，降低反应效率。
目前，对放射性固体废物的处理一般采用浓缩减容并使其与环境隔离(例如掩埋 等)的方式处理和处置。虽然采用超临界水氧化分解技术为当前有机废物处理研究的热点，但国内外未能够对固体废物进行超临界水氧化。究其原因之一为不能将放射性有机废料被切碎至足够小的颗粒度。而目前国内外对固体可燃物的粉碎由于粉碎工艺的限制，得到的碎块尺寸往往大于5mm；同时由于放射性有机废料的放射性污染，基本没有对放射性固体有机废料的切碎研磨工艺。这无疑会影响后续超临界水氧化处理技术的实施。究其原因之二在于高温高压设备的防护技术的缺乏。因此，研发能应用于高温高压反应设备的防护技术至关重要。
在相关技术中，超临界水氧化反应器处理的对象是液体废物，难以将固体废物进行超临界水氧化处理，无法解决例如核电站及其它核设施的放射性固体可燃废物的减容减害问题。
超临界水装备***没有形成一体机，超临界水氧化、流出物净化、防护设备等由不同设备完成，***集成不足，导致超临界水设备没有以工业产品的形式得到推广应用。再者，通常的超临界水技术反应温度普遍偏低，一般温度为500～600℃，低于有机物完全热解气化所需的最低温度(700℃左右)，也达不到难降解的有机物(如胺类等)完全无机化，从而使得超临界水氧化的优势发挥不足。
发明内容
为了解决现有技术的以上和其他方面的问题，本发明的实施例提供一种超临界水氧化***和固体废物处理方法。
本公开的一个方面提供了一种超临界水氧化反应器，包括壳体，内部形成用于提供反应区的腔室，上述壳体上至少设置有浆料入口、氧化剂入口和出料口；加热装置，用于提高上述腔室的温度；螺旋环流管，设置在上述腔室内，上述螺旋环流管的一端与上述浆料入口连通，其中，浆料从上述浆料入口导入上述螺旋环流管之后，沿上述螺旋环流管的管道流动，并从上述螺旋环流管的另一端流出；其中，上述浆料从上述螺旋环流管的另一端流出之后，与从上述氧化剂入口流入上述腔室的氧化剂混合并发生氧化反应。
根据本公开的实施例，超临界水氧化反应器还包括折返管，设置在上述腔室中，上述折返管包括两端开口的内管以及一端开口的外管，上述外管套设于上述内管的外部，上述内管与上述氧化剂入口连通。
根据本公开的实施例，上述折返管设置在上述腔室的中心轴位置。
根据本公开的实施例，超临界水氧化反应器还包括搅拌器，搅拌器包括转轴，上述转轴穿过上述壳体伸入上述腔室内，并且/或者上述转轴穿过上述出料口伸入上述腔室内。
根据本公开的实施例，其中，上述壳体包括第一端壁、侧壁以及与上述第一端壁相对的第二端壁，其中，上述浆料入口设置在上述侧壁上，上述氧化剂入口设置在上述第一端壁上，上述搅拌器和上述出料口设置在上述第二端壁上。
根据本公开的实施例，超临界水氧化反应器还包括内衬，设置在上述腔室中，其中，上述螺旋环流管沿上述内衬外壁缠绕设置，其中，上述内衬经渗铝、喷丸锻击以及喷涂热障涂层处理，上述热障涂层包括交替排布的多个铝层和多个氧化铝层。
根据本公开的实施例，超临界水氧化反应器还包括冷却装置，设置在上述侧壁上，用于冷却上述腔室中产生的反应产物；其中，上述加热装置与上述冷却装置并排设置在上述侧壁上，并且，上述加热装置与上述第一端壁的距离小于上述冷却装置与上述第一端壁的距离。
本公开的另一个方面提供了一种利用上述超临界水氧化反应器处理放射性有机废物的方法，该方法包括通过上述加热装置对上述腔室进行预加热；在上述腔室内的温度达到第一温度时，将目标溶液通过上述浆料入口输入上述腔室内，并对上述腔室继续加热，直到上述腔室内的温度达到第二温度；将上述放射性有机废物的浆料通过上述浆料入口输入上述螺旋环流管，沿上述螺旋环流管的管道流动，并从上述螺旋环流管的另一端流出；在上述放射性有机废物的浆料从上述螺旋环流管的另一端流出之后，与从上述氧化剂入口进入上述腔室的氧化剂混合并发生氧化反应。
根据本公开的实施例，上述方法还包括在上述超临界水氧化反应器包括折返管的情况下，上述氧化剂先从上述氧化剂入口进入上述折返管，在依次经过上述折返管的内管和外管之后，从上述外管的开口进入上述腔室。
根据本公开的实施例，在上述超临界水氧化反应器包括搅拌器的情况下，利用上述搅拌器对发生氧化反应之后得到氧化产物进行搅拌；
根据本公开的实施例，将上述氧化产物从上述出料口排出，其中，上述氧化产物从上述出料口排出时的温度为150℃至300℃之间，上述第二温度大于或等于600℃。
本公开的另一个方面提供了一种固体物料切碎机。该切碎机包括相互连通、依次设置的导料箱、切碎装置、料箱及胶体磨。其中，导料箱用于导入固体物料，并使固体物料沿导料箱的轴向方向下落。切碎装置包括能够在外力的驱动下转动的切刀，该 切碎装置用于通过切刀将沿导料箱的轴向方向落入的固体物料切成碎块。料箱用于通过导入到该料箱中的流动液体来带动自切碎装置中落入的碎块运动。该料箱的底部设置有包括多个筛孔的筛板，用于将部分的液体及尺寸小于多个筛孔的尺寸的碎块滤出料箱。胶体磨设置于筛板的下方，用于将滤出料箱的碎块研磨成浆料。
根据本公开的实施例，上述切碎装置包括切块组件，该切块组件包括固定筒、滚动筒及多个第一切刀。其中，固定筒的轴向方向垂直于导料箱的轴向方向，且固定筒包括第一侧壁，该第一侧壁上设置有相对应的第一开口与第二开口，分别用于连通导料箱与料箱。滚动筒沿固定筒的轴向方向设置于固定筒内，该滚动筒包括第二侧壁，第二侧壁与第一侧壁之间的距离与固体物料的尺寸相对应。多个第一切刀沿滚动筒的周向方向均匀设置于第二侧壁的外表面上，形成第一刀阵，用于将沿导料箱的轴向方向落入第一侧壁与第二侧壁之间的固体物料切成块状物。其中，第一刀阵中相邻两个第一切刀之间的距离被设置为与块状物的尺寸相对应。
根据本公开的实施例，上述切碎装置还包括粉碎组件。该粉碎组件设置于固定筒中滚动筒与料箱之间的位置，且该粉碎组件包括第二切刀，用于将落下的块状物切成碎块。其中，粉碎组件与第一侧壁之间的距离大于预设距离，以使碎块能够落入料箱。
根据本公开的实施例，上述第二切刀包括轴向切刀和径向切刀。其中，轴向切刀沿导料箱的轴向方向设置；径向切刀沿与导料箱的轴向方向及固定筒的轴向方向均垂直的方向设置。径向切刀与轴向方向共轴，且径向切刀位于轴向切刀与料箱之间。其中，轴向切刀和径向切刀被配置为在第一外力的作用下绕共轴的中心轴转动。
根据本公开的实施例，上述切块组件还包括多个第三切刀。该多个第三切刀沿固定筒的周向方向均匀设置于第一侧壁的内表面上，形成第二刀阵。上述滚动筒能够在第二外力的作用下绕其中心轴转动，以使沿导料箱的轴向方向落入第一侧壁与第二侧壁之间的固体物料在第一刀阵与第二刀阵的作用下被切成块状物。
根据本公开的实施例，上述滚动筒包括至少一组辊筒。该至少一组辊筒中的每组辊筒包括两个相对的辊筒，该两个相对的辊筒的侧壁均形成有第一刀阵，且两个相对的辊筒能够在第二外力的带动下向相反方向转动。其中，两个相对的辊筒之间的间距小于固体物料的尺寸。
根据本公开的实施例，上述多个第一切刀和/或多个第二切刀为多棱刀；并且/或者，上述第一刀阵中相邻两个第一切刀之间的距离和/或第二刀阵中相邻两个第三切刀之间的距离为分米量级。
根据本公开的实施例，上述导料箱包括相对设置的一对第三侧壁。该一对第三侧壁中的每个第三侧壁均设置有多个喷嘴，用于导入液体，使固体物料在该一对第三侧壁的多个喷嘴导入的液体的作用下沿导料箱的轴向方向下落。其中，每个第三侧壁与固定筒的轴向方向及导料箱的轴向方向均平行。
根据本公开的实施例，上述固体物料切碎机还包括导流装置。该导流装置用于驱动导入料箱中的流动液体流动，并将未滤出料箱的碎块及液体导流至导料箱。
根据本公开的实施例，上述碎块在任意一个方向的宽度小于5mm；并且/或者，上述浆料的颗粒度小于50μm。
本公开的另一个方面提供了一种反应设备的防护装置，该装置包括相对设置的一对防护端板以及防护组件。其中，防护组件设置于一对防护端板之间，且该防护组件包括外防护层、内防护层及冷却层。其中，外防护层与一对防护端板围成第一空间。内防护层设置于第一空间内且与一对防护端板围成用于容纳反应设备的第二空间。该内防护层在沿一对防护端板的连线方向上设置有多个导流孔，用于将反应设备的释放物导入外防护层与内防护层之间。冷却层夹设于内防护层与外防护层之间，该冷却层包括能够存储液体的液体管路。其中，防护组件被配置为：在第二空间中容纳有处于工作状态的反应设备的情况下，液体管路中存储有液体，第一空间为封闭空间。
根据本公开的实施例，上述一对防护端板包括第一防护端板和第二防护端板。其中，第一防护端板具有第一液体入口、第一液体出口及连通第一液体入口与第一液体出口的第一液体通路，第一液体入口在外力作用下能够打开或关闭，第一液体出口与液体管路连通，第一防护端板被配置为：在第一液体入口打开时，用于使从第一液体入口导入的液体流经第一液体通路，并自第一液体出口流入液体管路。第二防护端板具有第二液体入口、第二液体出口及连通第二液体入口与第二液体出口的第二液体通路，第二液体出口在外力作用下能够打开或关闭，第二液体入口与液体管路连通，第二防护端板被配置为：在第二液体出口打开时，用于使液体管路中的液体自第二冷却液入口流出液体管路，并流经第二液体通路后导出第二冷却液出口。其中，防护装置被配置为：在第二空间中容纳有处于工作状态的反应设备的情况下，第一液体入口与第二液体出口关闭，且第一液体通路与第二液体通路中存储有液体。
根据本公开的实施例，上述一对防护端板中的第一防护端板具有第一液体入口、第一液体出口及连通第一液体入口与第一液体出口的第一液体通路；上述一对防护端板中的第二防护端板具有第二液体入口、第二液体出口及连通第二液体入口与第二液 体出口的第二液体通路；以及上述液体管路包括多个第一管路，该多个第一管路在一对防护端板的连线方向上延伸设置，且多个第一管路在垂直于内防护层的方向及内防护层的周向方向周期排布。其中，上述多个第一管路具有相对设置的第一端和第二端，第一端与第一液体出口连通，第二端与第二液体入口连通。
根据本公开的实施例，上述液体管路还包括多个第二管路。该多个第二管路在内防护层的周向方向上延伸设置，且多个第二管路在一对防护端板的连线方向及垂直于所述内防护层的方向周期排布。其中，多个第二管路与多个第一管路经由多个管路连接件连通，防护装置被配置为：用于使从第一液体入口导入的液体依次流入第一液体通路、第一管路及第二管路。
根据本公开的实施例，上述第一防护端板包括第一端板、第二端板和第一筒体。其中，第一筒体设置于第一端板和第二端板之间，以在第一端板与第二端板之间围成第一液体通路，第一液体入口设置于第一筒体上，第一液体出口设置于第二端板上，且第二端板相对于第一端板靠近第二防护端板。
根据本公开的实施例，上述第二防护端板包括第三端板、第四端板和第二筒体。其中，第二筒体设置于第三端板和第四端板之间，以在第三端板与第四端板之间围成第二液体通路，第二液体出口设置于第一筒体上，第二液体出口设置于第三端板上，且第三端板相对于第四端板靠近第一防护端板。
根据本公开的实施例，上述第一端板和/或第二端板的厚度为30mm～70mm，上述第二筒体的高度为30mm～70mm；并且/或者，上述第三端板和/或第四端板的厚度为30mm～70mm，第二筒体的高度为30mm～70mm。
根据本公开的实施例，上述多个导流孔在内防护层上周期排布。
根据本公开的实施例，上述内防护层的厚度为30mm～50mm；上述外防护层的厚度为30mm～50mm；并且/或者，上述内防护层和/或外防护层的主体材质包括钢。
本公开的另一个方面提供了一种反应***，该反应***包括上述的反应设备的防护装置及反应设备。其中，反应设备放置于由防护装置的内防护层与一对防护端板围成的第二空间中。
根据本公开的实施例，上述反应设备包括超临界水反应设备。
本公开的另一个方面提供了一种超临界水氧化***，包括供水装置，用于提供水和目标溶液；氧化剂供料装置，用于为超临界水氧化反应提供氧化剂；固体可燃物切碎磨浆机，用于将固体可燃物磨碎至浆料；超临界水氧化反应器，用于接收上述固体 可燃物磨碎后得到的浆料、上述氧化剂、上述水和上述目标溶液，并提供超临界水氧化反应的反应区；分离设备，用于分离上述超临界水氧化反应器的流出物。
根据本公开的实施例，上述超临界水氧化反应器包括第一壳体，内部形成用于提供上述反应区的腔室，上述第一壳体上至少设置有浆料入口、氧化剂入口和出料口；加热装置，用于提高上述腔室的温度；螺旋环流管，设置在上述腔室内，上述螺旋环流管的一端与上述浆料入口连通，其中，上述螺旋环流管设置为使得上述浆料从上述浆料入口导入上述螺旋环流管之后，沿上述螺旋环流管的管道流动，从上述螺旋环流管的另一端流出，并与从上述氧化剂入口流入上述腔室的氧化剂混合并发生氧化反应。
根据本公开的实施例，上述超临界水氧化反应器还包括折返管，设置在上述腔室中，上述折返管包括两端开口的内管以及一端开口的外管，上述外管套设于上述内管的外部，上述内管与上述氧化剂入口连通。
根据本公开的实施例，上述折返管设置在上述腔室的中心轴位置。
根据本公开的实施例，上述超临界水氧化反应器还包括搅拌器，搅拌器包括转轴，上述转轴穿过上述第一壳体伸入上述腔室内，并且/或者上述转轴穿过上述出料口伸入上述腔室内；内衬，设置在上述腔室中，其中，上述螺旋环流管沿上述内衬外壁缠绕设置。
根据本公开的实施例，上述分离设备包括蒸发池，用于接收上述超临界水氧化反应器的流出物，其中，上述流出物为多态相混合物，其中，上述蒸发池内设置有第一冷却盘管和排渣口，上述第一冷却盘管用于在上述多态相混合物流入上述蒸发池之后，将上述蒸发池中溶液的温度稳定在目标温度范围内，上述排渣口用于排出上述多态相混合物中的固态物质；冷却内桶，包括第二冷却盘管和冷凝水池，上述第二冷却盘管用于冷却上述蒸发池中蒸发的蒸汽，上述冷凝水池用于接收上述第二冷却盘管冷却上述蒸汽后得到的液态物质，上述冷凝水池设置有排水口，用于排出上述液态物质，其中，上述冷却内桶的桶壁上设置有多个孔道，用于供上述蒸发池中蒸发的蒸汽进入上述冷却内桶；其中，上述蒸发池与上述冷却内桶封装在第二壳体内，上述蒸发池设置在上述冷却内桶下方，上述第二壳体的顶部设置有排气口，用于排放上述多态相混合物中的气态物质。
根据本公开的实施例，上述蒸发池内设置有用于接收上述多态相混合物的套管，上述套管的管壁上分布有多个小孔，上述多态相混合物通过上述多个小孔分散排入上述蒸发池内。
根据本公开的实施例，上述分离设备还包括背压阀，其中，上述背压阀一端通过管道与上述套管连接，上述背压阀另一端用于通过管道与上述超临界水氧化反应器的出料口连接；并且/或者上述排气口处设置有挥发性有机物在线监测器；并且/或者上述蒸发池内配备有液位计；并且/或者上述蒸发池内配备有pH计；并且/或者上述排水口处配备有化学需氧量在线监测器。
本公开的另一个方面提供了一种利用超临界水氧化***处理固体可燃物的方法，包括将上述超临界水氧化反应器的腔室温度提升到第一温度；通过上述氧化剂供料装置将氧化剂输入上述腔室内；通过上述供水装置将目标溶液输入上述腔室内，并对上述腔室继续加热，直到上述腔室内的温度达到第二温度；通过上述固体可燃物切碎磨浆机将固体可燃物磨碎至浆料，并将上述浆料输入上述腔室内，以使得上述浆料与上述氧化剂发生氧化反应，得到流出物；通过上述超临界水氧化反应器的出料口将上述流出物送入上述分离设备；以及通过上述分离设备分离上述流出物。
根据本公开的实施例，在上述分离设备分离上述流出物的过程中，上述方法还包括通过上述分离设备上设置的化学需氧量在线监测器监测排出的液态物质的COD值；并且/或者通过上述分离设备上设置的挥发性有机物在线监测器监测排出的气态物质的VOC值；并且/或者通过上述分离设备上设置的pH计监测上述分离设备中的蒸发池中溶液的pH值；并且/或者通过上述分离设备上设置的温度计监测上述分离设备中的蒸发池中溶液的温度和/或冷却内桶内的温度。
本公开另一个方面提供了一种超临界水氧化***。该***包括反应器、防护装置、氧化剂供给装置和有机物供料装置。其中，反应器包括反应器壳体，该反应器壳体上设置有氧化剂进料口、有机物进料口及出料口，反应器经由出料口排放反应产物。防护装置包括外防护层、冷却层及内防护层。其中，内防护层与外防护层围成有第一空间和第二空间，冷却层包括能够存储液体的液体管路，该液体管路设置于所述第一空间；反应器设置于第二空间，且反应器的出料口延伸至第一空间中除液体管路所在区域之外的区域，使得出料口排放的反应产物能够通过液体管路中存储的液体降温。氧化剂供给装置与氧化剂进料口相连通，有机物供料装置与有机物进料口相连通。
根据本公开的实施例，上述外防护层包括外套筒和相对设置的一对侧壁端板，内防护层包括共轴的第一筒体及相对设置的一对第二筒体，第一筒体设置于一对第二筒体之间，并与一对第二筒体共轴。其中，第一筒体包括第一筒体侧壁，且其为两端开口的结构。一对第二筒体中每个第二筒体包括第一端板和第二筒体侧壁，第一端板为 环形板结构，其内环尺寸与第一筒体的尺寸相匹配，且一对第二筒体经由第一端板与第一筒体固定连接。第一筒体侧壁、第一端板及外套筒围成上述第一空间，第一筒体、第二筒体及一对侧壁端板围成上述第二空间。上述液体管路包括沿一对侧壁端板的连线方向延伸设置的多个双层套管，该多个双层套管在外套筒的径向方向及外套筒的周向方向周期排布，且每个双层套管包括外层套管和内层套管。其中，第一端板上设置有多个第一接口，用于分别与多个双层套管的外层套管连通。
根据本公开的实施例，上述一对第二筒体中每个筒体的第二侧壁具有第一开口，其中一个第一开口作为第一进液口，另一个第一开口作为第一出液口。上述防护装置被配置为：在第二空间中设置的反应器处于工作状态时，液体循环地自第一进液口导入，并在流经多个双层套管的外层套管后，自第一出液口导出，以对出料口排放的反应产物进行降温。
根据本公开的实施例，上述一对第二筒体中每个第二筒体还包括与第一端板相对的第二端板、以及设置于第一端板和第二端板之间的分界板。上述第一开口设置于第一端板与分界板之间的侧壁上。上述分界板上设置有多个第二接口，用于分别与多个双层套管的内层套管连通。内层套管的长度大于外层套管，第二端板上设置有多个连通孔，用于使内层套管与第二空间相连通。其中，第二端板及分界板为与第一端板相同的环形板结构。
根据本公开的实施例，上述冷却层还包括多个气体管路和冷凝液收集盘。其中，冷凝液收集盘设置于第一空间中沿外套筒的径向方向周期排布的相邻两组双层套管之间，冷凝液收集盘在靠近出料口的第一盘面为封闭结构，且在远离出料口的第二盘面为开口结构。冷凝液收集盘具有在外套筒的轴向方向上周期排列的多个凹槽，且多个凹槽在垂直于第一盘面和第二盘面的连线方向延伸。多个气体管路沿第一盘面和第二盘面的连线方向上延伸设置于多个凹槽处，多个气体管路在靠近第一盘面的第一端为开口结构，靠近第二盘面的第二端为闭合结构，多个气体管路的第二端高出第二盘面，且多个气体管路在高出第二盘面的侧壁上具有多个喷气口。其中，外防护层设置有排渣口、排液口及排气口，分别用于排出反应产物中的残渣及反应产物降温得到的冷凝液及废气，排液口与冷凝液收集盘连通。
根据本公开的实施例，上述反应器壳体包括第一端壁、壳体侧壁以及与第一端壁相对设置的第二端壁。上述氧化剂进料口设置于第一端壁，出料口设置于第二端壁，有机物进料口设置于靠近第二端壁的壳体侧壁上。上述反应器还包括多根有机物输送 管及端部环管。多根有机物输送管沿第一端壁和第二端壁的连线方向延伸设置于反应器壳体内。上述多根有机物输送管包括第一端及与第一端相对的第二端，有机物输送管的第一端与有机物进料口连通。端部环管设置于反应器壳体内靠近第一端壁的区域，且端部环管与多根有机物输送管的第二端连通。其中，端部环管在靠近第二端壁的侧壁上设置有多个第一出料孔，并且/或者，上述多个有机物输送管在靠近反应器的中心轴、且靠近第一端壁的侧壁上设置有多个第二出料孔。
根据本公开的实施例，上述反应器还包括第三筒体和进料板。其中，第三筒体套设于多根有机物输送管及端部环管外部，且第三筒体包括第三端板及第三筒体侧壁。第三端板具有与氧化剂进料口相对应的第一进料孔。进料板设置于第三端板与端部环管之间，以在进料板与第三筒体之间形成氧化剂传输通道，且上述进料板上设置有多个第二进料孔。
根据本公开的实施例，上述壳体侧壁上还设置有第二进液口与第二出液口。上述反应器还包括内衬及环流套，内衬设置于壳体侧壁与第三筒体侧壁之间，环流套沿内衬在内衬与壳体侧壁之间螺旋缠绕设置。且上述环流套包括相对的第三端与第四端，第三端与第二进液口连通，第四端与第二出液口连通。
根据本公开的实施例，上述反应器还包括搅拌组件，该搅拌组件包括转轴，该转轴穿过反应器壳体及出料口。并且/或者，上述反应器壳体围成的空间可以分为靠近氧化剂进料口的第一区域及靠近有机物进料口及出料口的第二区域。上述反应器还包括加热组件和/或冷却组件，加热组件设置于第一区域的外部，用于提升反应器壳体内的温度，冷却组件设置于第二区域的外部，用于冷却氧化剂与有机物的反应产物。并且/或者，在上述反应器处于工作状态时，第一区域的中心温度为700℃～800℃。
根据本公开的实施例，上述有机物供应装置包括有机物供料组件、碱液箱、第一蠕动泵、第一高压泵和第一单向阀。上述第一蠕动泵与碱液箱连通，第一高压泵分别与碱液箱和第一蠕动泵相连通，第一单向阀设置于第一高压泵与有机物进料口之间。并且，上述有机物供料装置还包括蔗糖溶液箱、水箱、第二蠕动泵、第二高压泵和第二单向阀，第二蠕动泵与蔗糖溶液箱连通，第二高压泵分别与水箱和第二蠕动泵连通，第二单向阀设置于第二高压泵与有机物进料口之间。
根据本公开的实施例，上述有机物供料组件包括有机物切碎磨浆机，用于将固体有机物切碎研磨成浆料。该有机物切碎磨浆机包括相互连通且依次设置的倒料箱、剪切刀以及胶体磨。导料箱用于导入固体有机物及液体，导料箱的底部设置有导流孔。 剪切刀设置于导料箱的底部导流孔的上方，用于将下落的固体有机物切成1～5mm的碎渣。胶体磨用于将自导流孔流出的碎渣研磨成浆料。其中，上述剪切刀与胶体磨共轴，以在外力作用下同步转动。并且/或者，上述剪切刀包括一级剪切刀和二级剪切刀，该一级剪切刀用于将固体有机物切割成10～50mm的碎块，二级剪切刀用于将碎块切割成1～5mm的碎渣，二级剪切刀设置于一级剪切刀下方。
在相关技术中，一般在超临界水氧化反应器内将氧化剂和废料直接进行混合，然后待氧化剂和废料的温度达到一定温度之后才能完全发生反应。但是，由于有机料浆分子量大，分子空间结构稳定，难以在较短的时间内氧化。并且，在这种情况下，从外部输入的废料不仅会降低反应区的温度，导致废料在超临界水氧化反应器中的反应时间长，降低反应效率。通过本公开的实施例，在超临界水氧化反应器的腔室内设置了螺旋环流管，当超临界水氧化反应器的腔室内温度达到一定温度时，料浆在螺旋环流管内流动的过程中就可以进行充分预热，升温，甚至可以进行热分解，从而保障了有机料浆的热解时间，保证了有机料浆进行超临界水氧化的完全性，提高了反应效率。
本公开提供的固体物料切碎机，具有以下有益效果：
将对固体物料的导料、切碎和磨浆等功能集成于一体，可以将固体物料直接转化为浆料，因此具有处理能力大、集成度高的有益效果；且在处理放射性物质时，可以减少放射性操作环节；
通过向导料箱中导入液体，可以使得固体物料在液体环境下被切碎，因此可以避免气溶胶的产生；且由于固体物料可以在该导入流体的带动下沿轴向下落，即可以借助于液体的流动送料，而无需借助外力，因此可以充分利用空间，减小设备的整体大小；
大块物料采用辊筒上的刀阵切块，小块物料通过高速旋转的第三切刀切碎，从而可以将固体物料切碎至毫米量级，解决了现有技术中固体物料不能粉碎到毫米量级的技术瓶颈；且过滤出的碎块通过胶体磨研磨，可以达到浆料的颗粒度小、颗粒度均匀的有益效果。
本公开提供的反应设备的防护装置及反应***，具有以下有益效果：
通过防护组件的设置，可以将反应设备***而喷出的释放物导入外防护套与内防护套之间，则在该释放物与存储有液体的液体管路接触时，在压力差的作用下，释放物可以将液体管路冲爆，液体流出，从而起到对释放物降温减压的作用，避免释放物直接喷至外界环境导致的对环境的损害；
冷却层中通过互相连通的第一管路与第二管路的设置，可将该冷却层整体形成密集管路囚笼，因此在释放物导入冷却层时，可以增大管路与释放物的接触面积，并因此可以提高释放物降温减压的速度，将降温减压的整个过程控制在100s内，有效防止释放物对外防护层的冲击；
通过内防护层上周期排布的导流孔，可以实现对释放物的均匀分散，并因此避免释放物的集中冲击，进一步提高降温减压效率。
根据本公开的实施例，本公开的超临界水氧化***可以用于处理固体可燃物浆料。一般而言，如果固体直接进料超临界水氧化反应器会导致超临界水氧化反应器内堵塞，本公开突破了国内外进料为液体或气体的技术瓶颈，可以将固体经过切碎磨浆后，将浆料的颗粒低于50μm，浆料被泵入超临界水氧化反应器，为防止大颗粒在超临界水反应器内部沉积消除了障碍，解决了例如核电站及其它核设施的放射性固体可燃废物的减容减害问题。
本公开提供的超临界水氧化***，具有以下有益效果：
通过防护装置的设置，可以对反应产物进行有效降温，以将反应产物分离为残渣、冷凝液及废气。因此本公开实施例的超临界水氧化***，具有将超临界反应与反应产物冷却分离等功能集成为一体的一体机，而无需额外设置分离器，从而利于超临界水氧化技术的推广应用；
液体管路采用双层套管，并通过内防护层的设计，可将双层套管的内层套管与外层套管的空间隔离。在外层套管中走冷却液体，而内层套管与反应器所在的第二空间相连通。则在反应器因异常***，喷出高温高压的有机释放物时，该释放物可通过内防护层导入内层套管，与防护装置外部环境相隔离，并可通过外层套管中流动的液体实现冷却降温。因此，本公开实施例的超临界水氧化***，还集成有防护功能，可以有效防止异常释放物喷出防护装置外，因此集成度高，且可以有效避免异常释放物对外界环境的损害；
通过反应器中有机物输送管、端部环管的设计，可以保证有机物均匀的自端部及侧壁导入反应器中心室。并且通过进料板与第三筒体的的设计，可以保证氧化剂均匀的自端部及侧壁导入反应器中心室。从而可以使得有机物与氧化剂充分接触混合，使得反应器中心室的温度达到700℃～800℃。因此可以保证超临界水氧化反应优势的充分发挥，并有利于有机物的完全热解气化。
附图说明
为了更完整地理解本发明及其优势，现在将参考结合附图的以下描述，其中：
图1示意性示出了根据本公开实施例的超临界水氧化反应器的示意图；
图2示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图；
图3示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图；
图4示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图；
图5示意性示出了根据本公开实施例的冷却装置的示意图；
图6示意性示出了根据本公开实施例的利用超临界水氧化反应器处理放射性有机废物的流程图；
图7示意性示出了根据本公开第一实施例的固体物料切碎机的正视剖面图；
图8示意性示出了根据本公开第一实施例的固体物料切碎机的侧视剖面图；
图9示意性示出了根据本公开实施例的切碎装置的结构示意图；
图10A～图10B示意性示出了根据本公开实施例的第一切刀/第三切刀的结构示意图；
图11A～图11B示意性示出了根据本公开实施例的第二切刀的结构示意图；
图12示意性示出了根据本公开第二实施例的固体物料切碎机的正视剖面图；
图13示意性示出了根据本公开第三实施例的固体物料切碎机的正视剖面图；
图14示意性示出了根据本公开第一实施例的反应设备的防护装置的结构示意图；
图15A示意性示出了根据本公开实施例的一对防护端板中第一防护端板的结构示意图；
图15B示意性示出根据本公开实施例的一对防护端板中第二防护端板的结构示意图；
图16示意性示出了根据本公开第二实施例的反应设备的防护装置的结构示意图；
图17A示意性示出了参考图16中反应设备的防护装置的正视剖面图；
图17B示意性示出了参考图16中反应设备的防护装置的侧视剖面图；
图18示意性示出了根据本公开实施例的超临界水氧化***的示意图；
图19示意性示出了根据本公开实施例的利用超临界水氧化***处理固体可燃物的方法流程图；
图20示意性示出了根据本公开实施例的超临界水氧化反应器的示意图；
图21示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图；
图22示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图；
图23示意性示出了根据本公开实施例的冷却装置2206的示意图；
图24示意性示出了根据本公开实施例的分离设备的示意图；
图25示意性示出了根据本公开实施例的冷却内桶的示意图；
图26示意性示出了根据本公开实施例的套管的示意图；
图27示意性示出了根据本公开实施例的超临界水氧化***的结构示意图；
图28示意性示出了图27中的A-A剖面图；
图29示意性示出了参考图27中内防护层的结构示意图；
图30示意性示出了根据本公开实施例的反应器的主视截面图；
图31示意性示出了参考图30中虚线框区域结构的放大图；
图32A示意性示出了参考图31中的B-B剖视左视图；
图32B示意性示出了参考图31中的B-B剖视右视图；
图33示意性示出了本公开实施例的有机物供料装置的结构示意图；
图34示意性示出了本公开实施例的旋切磨浆机的结构示意图；以及
图35示意性示出了参考图34中旋切磨浆机的俯视图。
具体实施方式
以下，将参照附图来描述本公开的实施例。但是应该理解，这些描述只是示例性的，而并非要限制本公开的范围。在下面的详细描述中，为便于解释，阐述了许多具体的细节以提供对本公开实施例的全面理解。然而，明显地，一个或多个实施例在没有这些具体细节的情况下也可以被实施。此外，在以下说明中，省略了对公知结构和技术的描述，以避免不必要地混淆本公开的概念。
在此使用的术语仅仅是为了描述具体实施例，而并非意在限制本公开。在此使用的术语“包括”、“包含”等表明了所述特征、步骤、操作和/或部件的存在，但是并不排除存在或添加一个或多个其他特征、步骤、操作或部件。
在此使用的所有术语(包括技术和科学术语)具有本领域技术人员通常所理解的含义，除非另外定义。应注意，这里使用的术语应解释为具有与本说明书的上下文相一致的含义，而不应以理想化或过于刻板的方式来解释。
在使用类似于“A、B和C等中至少一个”这样的表述的情况下，一般来说应该按照本领域技术人员通常理解该表述的含义来予以解释(例如，“具有A、B和C中至 少一个的***”应包括但不限于单独具有A、单独具有B、单独具有C、具有A和B、具有A和C、具有B和C、和/或具有A、B、C的***等)。在使用类似于“A、B或C等中至少一个”这样的表述的情况下，一般来说应该按照本领域技术人员通常理解该表述的含义来予以解释(例如，“具有A、B或C中至少一个的***”应包括但不限于单独具有A、单独具有B、单独具有C、具有A和B、具有A和C、具有B和C、和/或具有A、B、C的***等)。
本公开的实施例提供了一种超临界水氧化反应器，包括壳体，内部形成用于提供反应区的腔室，壳体上至少设置有浆料入口、氧化剂入口和出料口；加热装置，用于提高腔室的温度；螺旋环流管，设置在腔室内，螺旋环流管的一端与浆料入口连通，其中，浆料从浆料入口导入螺旋环流管之后，沿螺旋环流管的管道流动，并从螺旋环流管的另一端流出；其中，浆料从螺旋环流管的另一端流出之后，与从氧化剂入口流入腔室的氧化剂混合并发生氧化反应。
图1示意性示出了根据本公开实施例的超临界水氧化反应器的示意图。需要注意的是，图1所示仅为可以应用本公开实施例的超临界水氧化反应器的示例，以帮助本领域技术人员理解本公开的技术内容，但并不意味着本公开的超临界水氧化反应器不可以是其它构造方式。
如图1所示，超临界水氧化反应器100包括壳体101，加热装置102和螺旋环流管103。
壳体101内部形成用于提供反应区的腔室，壳体101上至少设置有浆料入口1011、氧化剂入口1012和出料口1013。
根据本公开的实施例，壳体101可以包括外壳和内壳(例如，内壳可以是图1中的内衬1014)，外壳和内壳的形状、材质、尺寸大小不做限定。例如，壳体101的主体部分可以是圆柱型，外壳内径为80～219mm，长度1000～9000mm；内壳内径40～133mm，长度1000～9000mm。
加热装置102用于提高腔室的温度。根据本公开的实施例，加热装置102的类型不做限定。例如，加热装置102可以是加热套。本公开可以将加热套套设在壳体101的外壁，通过热传导的方式将热量传递给壳体101内部的腔室，当然本公开也不限定其它加热方式。根据本公开的实施例，超临界水氧化反应器100的外壳两端可以配备压力表，内壳两端与中间可以配备温度探头，加热套与外壳外壁之间可以配备温度探头。
根据本公开的实施例，加热装置102可以覆盖壳体101外壁的一部分。例如，加热装置102可以设置在螺旋环流管103流出浆料的出口所在的预定区域对应的外壁上，从而覆盖壳体101的一部分。具体地，如图1所示，加热装置102包括4块加热套，覆盖壳体101的中间至螺旋环流管103流出浆料的出口的区域。
螺旋环流管103设置在腔室内，螺旋环流管一端1031与浆料入口1011连通，其中，浆料从浆料入口1011导入螺旋环流管103之后，沿螺旋环流管103的管道流动，并从螺旋环流管另一端1032流出，其中，浆料从螺旋环流管1032流出之后，与从氧化剂入口1012流入腔室的氧化剂混合并发生氧化反应。需要说明的是，图1中关于螺旋环流管103中的环流管仅仅是示意性地，本公开不限定环流管的长度和绕圈数。
根据本公开的实施例，螺旋环流管103可以将有机浆料沿着环流管流动，一方面增加有机浆料的流动程度，另一方面增加有机浆料的流速，这样可以增加有机浆料的热解效率。
根据本公开的实施例，螺旋环流管103可以设置在贴近壳体101内壁的位置。具体地，在壳体101包括外壳和内壳的情况下，可以将螺旋环流管103可以设置在外壳和内壳之间。为了加大有机浆料的流动程度，可以将螺旋环流管103缠绕内壳进行设置。根据本公开的实施例，内壳也可以称之为内衬，如图1所示，内衬位置可以如图1所示设置。
根据本公开的实施例，本公开的超临界水氧化反应器100可以用于处理固体可燃物浆料。通过将固体可燃物切碎磨浆，直接导入螺旋环流管103中，可以实现在螺旋环流管103中进行热分解，从螺旋环流管103流出之后，就可以进行超临界水氧化反应。当超临界水的平均温度为600℃时，有机物热解一般为1秒左右，当有机物流量为10L/h，有机物停留时间最少8s以上，效果好于理论所需。
在相关技术中，如果有机物直接进料，则有机物会冷却反应区温度，减低反应效果。当反应温度为600℃时，有机物热解需要时间为1s左右，当反应温度为550℃时，有机物热解所需时间则为5min，会降低反应效率。可见，本公开相比于现有技术，反应时间非常快，提高了处理效率。
在相关技术中，一般在超临界水氧化反应器内将氧化剂和废料直接进行混合，然后待氧化剂和废料的温度达到一定温度之后才能完全发生反应。但是，由于有机料浆分子量大，分子空间结构稳定，难以在较短的时间内氧化。并且，在这种情况下，从外部输入的废料不仅会降低反应区的温度，导致废料在超临界水氧化反应器中的反应 时间长，降低反应效率。通过本公开的实施例，在超临界水氧化反应器的腔室内设置了螺旋环流管，当超临界水氧化反应器的腔室内温度达到一定温度时，料浆在螺旋环流管内流动的过程中就可以进行充分预热，升温，甚至可以进行热分解，从而保障了有机料浆的热解时间，保证了有机料浆进行超临界水氧化的完全性，提高了反应效率。
下面参考图2～图5，结合具体实施例对图1所示的反应器做进一步说明。
图2示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图。
如图2所示，超临界水氧化反应器200包括壳体201、加热装置202、螺旋环流管203和折返管204。
其中，壳体201上设置有浆料入口2011、氧化剂入口2012和出料口2013。螺旋环流管203包括螺旋环流管一端2031和螺旋环流管另一端2032。
需要说明的是，本公开实施例中的壳体201、加热装置202、螺旋环流管203可以参考本公开对图1的描述，为了描述的简洁起见，在此不再赘述。
根据本公开的实施例，折返管204设置在腔室中，折返管204包括两端开口的内管2041以及一端开口的外管2042，外管2042套设于内管2041的外部，内管2041与氧化剂入口2012连通。
根据本公开的实施例，氧化剂从氧化剂入口2012导入后，经过内管2041，然后进入外管2042，最后从外管2042的一端开口处导出。
根据本公开的实施例，折返管204可以设置在腔室的中心轴位置。
根据本公开的实施例，内管2041和外管2042的形状、材质、尺寸大小不做限定。例如，内管2041直径可以是φ25～φ42mm，壁厚可以是4～6mm，外管直径可以是42mm以上，壁厚可以是4～6mm，长度都可以在3000mm～6000mm之间。根据本公开的实施例，折返管204大小适中，可以有效降低生产成本，有利于市场应用。
根据本公开的实施例，折返管可以使得管内氧化剂尽可能升温，增加了预热时间。同时将折返管设置于超临界水反应器中心轴位置，使其受热温度可以达到最高。
根据本公开的实施例，氧化剂的种类不做限定。例如，可以是液氧，双氧水等等。
图3示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图。
如图3所示，超临界水氧化反应器300包括壳体301、加热装置302、螺旋环流管303、折返管304和搅拌器305。
其中，壳体301上设置有浆料入口3011、氧化剂入口3012和出料口3013。螺旋环流管303包括螺旋环流管一端3031和螺旋环流管另一端3032。折返管304包括两 端开口的内管3041以及一端开口的外管3042。
需要说明的是，本公开实施例中的壳体301、加热装置302、螺旋环流管303和折返管304等可以参考本公开对图1和/或图2的描述，为了描述的简洁起见，在此不再赘述。
根据本公开的实施例，搅拌器305包括转轴3051，转轴3051穿过壳体301伸入腔室内，并且/或者转轴3051穿过出料口3013伸入腔室内。
根据本公开的实施例，需要说明的是，搅拌器305还可以包括转子、隔离套、磁块等等搅拌器所需部件(图3中未示出)。
根据本公开的实施例，浆料入口3011、氧化剂入口3012和出料口3013的设置位置不做限定。
根据本公开的实施例，壳体301包括第一端壁、侧壁以及与第一端壁相对的第二端壁，其中，浆料入口3011设置在侧壁上，氧化剂入口3012设置在第一端壁上，搅拌器305和出料口3013设置在第二端壁上，可选地，出料口3013也可以设置在侧壁上。
根据本公开的实施例，搅拌器305可以是磁力搅拌器，在超临界水氧化反应器300竖直安装的情况下，可以通过将其安装于超临界水氧化反应器300的底部，主要用于搅拌反应器底部沉积物，防止出现固体颗粒物沉积、板结、堵塞出料口。
根据本公开的实施例，本公开的超临界水氧化反应器300可以用于处理固体可燃物浆料。一般而言，如果固体直接进料超临界水氧化反应器会导致超临界水氧化反应器内堵塞，本公开突破了国内外进料为液体或气体的技术瓶颈，可以将固体经过切碎磨浆后，将浆料的颗粒低于50μm，浆料被泵入超临界水氧化反应器，为防止大颗粒在超临界水反应器内部沉积消除了障碍。同时，在超临界水反应器浆料的输送通道上，设置了螺旋环流通道，使得浆料流速局部增大，避免了浆料沉积。进一步地，在超临界水氧化反应器内设置搅拌器，伸入腔室内，避免了浆料颗粒在超临界水反应器内部沉积。不仅实现了固体颗粒氧化完全彻底，而且避免了超临界水氧化反应器内堵塞。
根据本公开的实施例，超临界水氧化反应器还可以包括内衬。该内衬可以相当于超临界水氧化反应器的内壳。
根据本公开的实施例，可以将内衬设置在腔室中，其中，螺旋环流管可以沿内衬外壁缠绕设置。内衬可以经渗铝、喷丸锻击以及喷涂热障涂层处理，热障涂层包括交替排布的多个铝层和多个氧化铝层。
根据本公开的实施例，内衬经渗铝、喷丸锻击以及喷涂热障涂层处理，热障涂层包括交替排布的多个铝层和多个氧化铝层之后，相当于在内衬上生成了防腐涂层，可以使得通过超临界水的高温作用在内衬的内壁形成一层致密的凝胶层，阻止超临界水与内衬金属的接触与腐蚀。
根据本公开的实施例，形成致密的凝胶层的关键条件是在金属与凝胶层之间有一层致密的特殊金属原子。一方面，这层特殊的金属原子通过金属键与本体金属相连。另一方面又以化学键的形式与凝胶层相连。为了制备这层金属原子，本发明采用镍基金属，首先对金属本体进行渗铝处理，之后用喷丸锻击金属表面，以便形成致密的金属铝原子层，之后喷涂热障涂层，通过金属铝、三氧化二铝陶瓷层的交替喷涂，金属表面形成6～8层的热障涂层，厚度约2～3mm。热障涂层遇到超临界水后，这层热障涂层将转变为致密的凝胶层。凝胶层可以阻止超临界水与内衬金属的接触与腐蚀。
图4示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图。
如图4所示，超临界水氧化反应器400包括壳体401、加热装置402、螺旋环流管403、折返管404、搅拌器405和冷却装置406。
其中，壳体401上设置有浆料入口4011、氧化剂入口4012和出料口4013。螺旋环流管403包括螺旋环流管一端4031和螺旋环流管另一端4032。折返管404包括两端开口的内管4041以及一端开口的外管4042。搅拌器405包括转轴4051。
需要说明的是，本公开实施例中的壳体401、加热装置402、螺旋环流管403、折返管404和搅拌器405等可以参考本公开对图1、图2和图3的描述，为了描述的简洁起见，在此不再赘述。
冷却装置406设置在侧壁上，用于冷却腔室中产生的反应产物；其中，加热装置402与冷却装置406可以并排设置在侧壁上，并且，加热装置402与第一端壁的距离小于冷却装置406与第一端壁的距离。
根据本公开的实施例，如图4所示，加热装置402与第一端壁的距离小于冷却装置406与第一端壁的距离，也即，加热装置402更靠近第一端壁，冷却装置406远离第一端壁。由于浆料和氧化剂在靠近第一端壁的位置发生反应，因此，可以在靠近第一端壁的位置设置加热装置402，可以在靠近第二端壁的位置设置冷却装置406。
图5示意性示出了根据本公开实施例的冷却装置406的示意图。
如图5所示，冷却装置406可以由冷却套组组成，覆盖在超临界水氧化反应器400的外壁，每个冷却套组包括2个半冷却套4061，2个半冷却套4061可以以固定孔和螺 栓4062固定，半冷却套4061中可以充入冷却水，例如按照图5中箭头方式从2个半冷却套4061一端充入水后，然后从2个半冷却套4061另一端排出水。
根据本公开的实施例，需要说明的是，冷却装置406在冷却腔室中产生的反应产物时，一般不会将反应产物的温度降低到常温，可以是将反应产物的温度降低到比常温高，甚至是高于水沸腾的温度，例如，从500℃降低到300℃，如此设计，由于反应产物排出时的温度较高，不仅减轻了超临界水反应器降温的负担，同时提高超临界水氧化反应器流出物温度后，可以充分利用反应产物自身的温度为后面的反应产物分离设备创造了自发蒸发的必要条件。需要说明的是，冷却装置406的另一个功能是防止腔室的温度过高，从而防止过热反应。
根据本公开的实施例，还提供了一种利用超临界水氧化反应器处理放射性有机废物的方法。根据本公开的实施例，处理放射性有机废物所需的超临界水氧化反应器可以是本公开图1至图4中任一所述的超临界水氧化反应器。
在相关技术中，一般在超临界水氧化反应器内将氧化剂和废料直接进行混合，然后待氧化剂和废料的温度达到一定温度之后才能完全发生反应。但是，由于有机料浆分子量大，分子空间结构稳定，难以在较短的时间内氧化。并且，在这种情况下，从外部输入的废料不仅会降低反应区的温度，导致废料在超临界水氧化反应器中的反应时间长，降低反应效率。通过本公开的实施例，在超临界水氧化反应器的腔室内设置了螺旋环流管，当超临界水氧化反应器的腔室内温度达到一定温度时，放射性有机废物在螺旋环流管内流动的过程中就可以进行充分预热，升温，甚至可以进行热分解，从而延长了放射性有机废物的热解时间，保证了放射性有机废物进行超临界水氧化的完全性，提高了反应效率。
图6示意性示出了根据本公开实施例的利用超临界水氧化反应器处理放射性有机废物的流程图。
如图6所示，利用超临界水氧化反应器处理放射性有机废物包括步骤S601～S604。
在步骤S601，通过加热装置对腔室进行预加热。
步骤S602，在腔室内的温度达到第一温度时，将目标溶液通过浆料入口输入腔室内，并对腔室继续加热，直到腔室内的温度达到第二温度。
根据本公开的实施例，例如，可以利用电加热套预热反应器，使反应器腔室内的温度达到第一温度，例如可以是300℃。根据本公开的实施例，目标溶液可以是蔗糖溶液，可以启动蔗糖溶液供料泵，将蔗糖溶液通过浆料入口输入腔室内，将反应器温 度加热到第二温度，其中，第二温度大于或等于600℃，例如可以是650℃以上。
根据本公开的实施例，在超临界水氧化反应器包括折返管的情况下，氧化剂先从氧化剂入口进入折返管，在依次经过折返管的内管和外管之后，从外管的开口进入腔室。
步骤S603，将放射性有机废物的浆料通过浆料入口输入螺旋环流管，沿螺旋环流管的管道流动，并从螺旋环流管的另一端流出。
根据本公开的实施例，在达到反应条件的情况下，例如，超临界水氧化温度保持在650℃～750℃，压力保持在20～25Mpa的情况下，启动有机废物供料泵，将放射性有机废物的浆料通过浆料入口输入螺旋环流管。一般工况下，反应器内壳靠近喷嘴部分温度为650℃～800℃，相对应外壳部分温度不超过600℃，经过内外壳加套与外壳加套的双重冷却后，反应产物温度降低到120℃～300℃以下，但不应太低，应该有足够的温度将反应产物自身能够全部蒸发。
步骤S604，在放射性有机废物的浆料从螺旋环流管的另一端流出之后，与从氧化剂入口进入腔室的氧化剂混合并发生氧化反应。
根据本公开的实施例，在超临界水氧化反应器包括搅拌器的情况下，利用搅拌器对发生氧化反应之后得到的氧化产物进行搅拌。
根据本公开的实施例，将氧化产物从出料口排出时，氧化产物从出料口排出时的温度为可以是120℃至300℃之间，可选地，可以是150℃至300℃之间。
根据本公开的实施例，相关技术中一般反应温度为600℃，本公开相比其它超临界水反应的反应温度高，有效提高了反应速率。同时，氧化产物的出口温度高，可以是300℃，减轻了超临界水反应器的负担。对于固体可燃物处理能力可以达到20～200kg/h，甚至更高处理水平。
本公开可以利用超临界水氧化反应器处理固体可燃物浆料。通过将固体可燃物切碎磨浆，直接导入螺旋环流管中，可以实现在螺旋环流管中进行热分解，从螺旋环流管流出之后，就可以进行超临界水氧化反应。当超临界水的平均温度为600℃时，有机物热解一般为1秒左右，当固体可燃物流量为10L/h，有机物停留时间最少8s以上，效果好于理论所需。
本公开的实施例提供了一种固体物料切碎机。该固体物料切碎机包括相互连通、依次设置的导料箱、切碎装置、料箱及胶体磨。其中，导料箱用于导入固体物料，并 使固体物料沿导料箱的轴向方向下落；切碎装置包括能够在外力的驱动下转动的切刀，该切碎装置用于通过切刀将沿导料箱的轴向方向落入的固体物料切成碎块；料箱用于通过导入到料箱中的流动液体来带动自切碎装置中落入的碎块运动；料箱的底部设置有包括多个筛孔的筛板，用于将部分的液体及尺寸小于多个筛孔的尺寸的碎块滤出料箱；胶体磨设置于筛板的下方，用于将滤出料箱的碎块研磨成浆料。
图7～图8示意性示出了根据本公开第一实施例的固体物料切碎机的结构示意图。其中，图7为该固体物料切碎机的正视剖面图，图8为该固体物料切碎机的侧视(左视或右视)剖面图。
如图7所示，本公开实施例的固体物料切碎机1包括相互连通、依次设置的导料箱10、切碎装置20、料箱30及胶体磨40。
其中，导料箱10用于导入固体物料，并使固体物料沿导料箱1的轴向方向(即参考图7中的竖直方向)下落。根据本公开的实施例，该导料箱具体例如可以是长方体形状的导料箱。该导料箱在轴向方向上靠近切碎装置20的一端例如可以是开口结构，以便于固体物料落入切碎装置。
其中，切碎装置20包括能够在外力的驱动下转动的切刀，则该切碎装置20用于通过切刀将沿导料箱10的轴向方向落下的固体物料切成碎块。根据本公开的实施例，如图7～8所示，所述的外力例如可以是由第一电机2和/或第二电机3提供的外力。
根据本公开的实施例，如图7～8所示，切碎装置20例如可以包括有切块组件21，该切块组件21用于将固体物料切成块状物。根据本公开的实施例，该切块组件21包括有上述能够在外力驱动下转动的切刀，此种情况下，所述外力由第二电机3提供。
根据本公开的实施例，切碎装置20例如还可以包括有粉碎组件22，该粉碎组件22用于对切块组件21切成的块状物进行进一步的切割，得到碎块。根据本公开的实施例，该粉碎组件22例如也可以包括有上述能够在外力驱动下转动的切刀，此种情况下，所述外力不仅由第二电机3提供，还有第一电机2提供。其中，第二电机3用于驱动切块组件21包括的切刀转动，第一电机2用于驱动粉碎组件22包括的切刀转动。
根据本公开的实施例，该切碎装置20例如可以具有外壳，则切碎组件21和粉碎组件22设置于该外壳中。该外壳可以与导料箱10与料箱30一体成型。
其中，料箱30具体用于通过导入到料箱30中的流动液体来带动自切碎装置20中落入的碎块运动。再者，该料箱30的底部设置有包括多个筛孔的筛板31，流动液体能够带动落入的碎块运动至筛板31所在区域，此时，尺寸小于多个筛孔尺寸的碎块 即可随着部分的液体被滤出料箱30，以便于采用胶体磨40进行研磨。根据本公开的实施例，该筛板31的筛孔尺寸具体可以根据胶体磨40的需求进行设定，例如该筛孔尺寸可以小于5mm。相应地，由上述切碎装置20切碎得到的碎块中至少部分的碎块应该能够满足在任意一个方向的宽度都小于5mm的要求。
根据本公开的实施例，切碎装置20与料箱30之间例如可以设置有碎块物料导流孔50，以将切碎装置20切成的碎块顺利的导入料箱30中。
其中，胶体磨40设置于料箱30底部设置的筛板31的下方，以对滤出料箱30的碎块进行研磨。考虑到随着碎块滤出的还有料箱中流动的液体，因此胶体磨40在对碎块进行研磨时，无需再另外添加液体。碎块在胶体磨40的研磨作用下成为浆料，具体例如可以转化为胶体粒子。根据本公开的实施例，该胶体磨40的类型具体可以根据实际需求进行选择，以使得研磨得到的浆料的颗粒度满足实际需求。其中，研磨得到的浆料的颗粒度具体例如可以低于50μm。
综上可知，本公开实施例的固体物料切碎机，可以直接将固体物料切碎研磨成浆料，因此集成度高，处理效率高。且由于该固体物料切碎机通过设置切碎装置及胶体磨，将切碎与研磨等功能集成为一体，因此在固体物料为放射性可燃废物时，可以有效的减少放射性操作环节，从而降低放射性污染。
图9示意性示出了根据本公开实施例的切碎装置的结构示意图。
如图9所示，本公开实施例的切碎装置20具体包括有切块组件21和粉碎组件22。
其中，切块组件21包括固定筒211、滚动筒212及多个第一切刀213。
其中，固定筒211的轴向方向垂直于导料箱10的轴向方向，该固定筒211的轴向方向具体例如可以既垂直于参考图1中的竖直方向又垂直于导料箱10的宽度方向。如图9所示，该固定筒211包括第一侧壁2111，该第一侧壁2111上设置有相对应的第一开口215和第二开口216，该两个开口分别用于连通导料箱10和料箱30。具体地，该第一侧壁2111设置第一开口215的部分可以与导料箱10的开口结构的侧壁相接，以使得导料箱10与切块组件21经由开口结构与第一开口215连通，从而使得导料箱10导入的固体物料落入固定筒211中。
其中，滚动筒212沿固定筒211的轴向方向设置于固定筒211内。该滚动筒212包括有第二侧壁2121，该第二侧壁2121与第一侧壁2111之间的距离具体可以与固体物料的尺寸相对应，以使得自导料箱10落入的固体物料能够下落至滚动筒212与固定筒211之间。
其中，多个第一切刀213具体可以沿滚动筒212的周向方向(即围绕滚动筒212的中心轴的方向)设置于第二侧壁2121上。具体地，该多个第一切刀213可以是在第二侧壁2121上均匀排列设置，以形成第一刀阵。则在固体物料落入滚动筒212与固定筒211之间(即第一侧壁2111与第二侧壁2121之间)时，在第一刀阵的切割作用下，即可将固体物料切成块状物。
根据本公开的实施例，上述滚动筒212与固定筒211的尺寸具体可以根据固体物料的尺寸而选择设置，以使得第一侧壁2111与第二侧壁2121之间的距离不会因太小而无法落入固体物料，也不会因太大使得落入的固体物料直接沿第一侧壁2111与第一刀阵之间的孔隙落下而未被切割。
根据本公开的实施例，上述第一刀阵中相邻两个第一切刀213之间的距离具体可以根据切割需求进行设定，即该距离与切成的块状物的尺寸相对应。当需要将固体物料切成较小尺寸时，则可以适当的减小两个相邻的第一切刀之间的距离，而在需要将固体物料切成较大尺寸时，则可以适当的增大两个相邻的第一切刀之间的距离。根据本公开的实施例，该相邻两个第一切刀213之间的距离例如可以为分米量级，例如可以为100mm。
根据本公开的实施例，如图9所示，该切块组件21例如还可以包括多个第三切刀214。该多个第三切刀214可以沿固定筒211的周向方向设置于第一侧壁2111的内表面上，以与多个第一切刀213相对设置。具体地，该多个第三切刀214例如可以是在第一侧壁2111上均匀排列设置的，以形成第二刀阵。
根据本公开的实施例，上述的滚动筒212具体可以在第二外力的作用下绕其中心轴转动，以使沿导料箱10的轴向方向落入该第一侧壁2111与第二侧壁2121之间的固体物料能够在第一刀阵和第二刀阵的作用下被切成块状物。具体地，当固体物料落入该第一侧壁2111与第二侧壁2121之间时，该固体物料被卡置于相邻的多个第一切刀213之间。则随着滚动筒212的转动，该固体物料随着转动，并在第二刀阵中的第三切刀214的作用下被不断切割细化，从而被切割成尺寸小于第一侧壁2111与第二侧壁2121之间的距离的块状物。并因此实现对固体物料的有效切割，并将固体物料切成的块状物的尺寸限制在一定范围内(例如100mm范围内)。根据本公开的实施例，该第二刀阵中两个相邻的第三切刀214之间的距离例如可以与两个相邻的第一切刀213之间的距离相等或不等。根据本公开的实施例，该两个相邻的第三切刀214之间的距离例如也可以为分米量级。
根据本公开的实施例，上述第二外力具体可以是由参考图8中的第二电机3提供，该滚动筒212在该第二外力作用下慢速转动，转动速度具体可以是5R/min～50R/min。本公开对该滚动筒212的转动速度不作限定，该滚动筒212的转动速度具体可以根据固体物料的硬度及切割需求进行设定。
根据本公开的实施例，如图9所示，该滚动筒212具体例如可以包括有沿固定筒211的轴向方向排布的至少一组辊筒。每组辊筒包括有两个相对的辊筒，且该两个相对的辊筒的侧壁均形成有第一刀阵。根据本公开的实施例，该两个相对的辊筒例如能够在上述第二外力的带动下向相反方向转动，以将落入该两个辊筒之间的固体物料带至第一刀阵与第二刀阵之间，实现固体物料的切割。
根据本公开的实施例，该两个相对的辊筒例如可以相对于导料箱的中心轴对称设置，且该两个相对的辊筒之间的间距应小于固体物料的尺寸，以避免沿导料箱的轴向方向落入的固体物料直接沿两个相对的辊筒之间的间距掉落至粉碎组件22或料箱30中。
其中，如图9所示，上述粉碎组件22可以设置在固定筒211中滚动筒212与料箱30之间的位置，以对经由切块组件21得到的块状物进行进一步的切割，得到固体物料的碎块。
根据本公开的实施例，该粉碎组件22与固定筒211的第一侧壁2111之间的距离需要大于预设距离，以便于使粉碎组件22切割后得到的碎块能够经由该第一侧壁2111与粉碎组件22之间的空间落入料箱30。其中，所述预设距离具体可以根据粉碎组件22切割得到的碎块的大小进行设定。该预设距离也不宜过大，以防止经由切块组件22得到的块状物直接经由粉碎组件22与第一侧壁2111之间的距离落入料箱30。根据本公开的实施例，该预设距离例如可以为5mm。
根据本公开的实施例，该粉碎组件22例如可以包括有第二切刀，用于将块状物切成碎块，进一步地减小进入料箱30的碎块的尺寸，为胶体磨40的研磨提供条件。其中，该第二切刀例如可以在第一外力的作用下高速转动，以保证对块状物的有效切割。其中，该第一外力例如可以由参考图7～图8中所示的第一电机2提供。该第二切刀的转动速度具体可以根据固体物料的硬度等进行设置，例如该第二切刀的转动速度可以为1000R/min～3000R/min。
根据本公开的实施例，该粉碎组件22的第二切刀具体例如可以包括有轴向切刀221和径向切刀222。其中，轴向切刀221沿着导料箱10的轴向方向设置，而径向切 刀222沿着与导料箱10的轴向方向及固定筒211的轴向方向均垂直的方向设置。进一步地，径向切刀222例如可以与轴向切刀221共轴，以使得该径向切刀222与轴向切刀221在第一外力的作用下绕共轴的中心轴同步转动。具体地，径向切刀222可以位于轴向切刀221与料箱30之间，以对由轴向切刀221轴向切割后的块状物进行进一步的径向切割，使得最终得到的碎块尺寸大约小于5mm，为碎块进入胶体磨做好准备。
综上可知，本公开实施例的切碎装置，通过采用大块物料经由慢速旋转的辊筒刀阵切块，小块物料经由高速旋转的切刀旋切相结合的切碎方法，可以将得到碎块尺寸减小至5mm以内，且得到的碎块均匀性好，从而为该碎块进入胶体磨被研磨成浆料做好准备。
图10A～图10B示意性示出了根据本公开实施例的第一切刀/第三切刀的结构示意图。其中，图10A为该第一切刀/第三切刀的正视图，图10B为该第一切刀/第三切刀的俯视图。
根据本公开的实施例，上述形成第一刀阵的第一切刀和/或形成第二刀阵的第二切刀例如可以采用多棱刀结构，以提高第一刀阵与第二刀阵的稳固性及锋利度，提高切割效率。具体地，如图10A～图10B所示，该第一切刀/第三切刀为四棱刀。
图11A～图11B示意性示出了根据本公开实施例的粉碎组件的结构示意图。其中，图11A为第二切刀的正视图，图11B为第二切刀的俯视图。
根据本公开的实施例，如图8所示，上述粉碎组件22例如可以为周期排列的多个，多个粉碎组件22沿着参考图9中固定筒211的中心轴周期分布，以对沿固定筒211的中心轴的方向上不同位置处掉落的块状物进行切割。每个粉碎组件22均包括有第二切刀，第二切刀具有轴向切刀221和径向切刀222。相应地，参考图8中的第一电机2的数量应与粉碎组件22的个数相同。
如图11A～图11B所示，上述第二切刀中的轴向切刀221例如可以设置为具有不同高度的多对轴向切刀，每对切刀中的两个切刀沿着轴向切刀221和径向切刀222的共轴的中心轴223对称设置，以对块状物进行分级切割。具体可以是，块状物先被高度高的轴向切刀切割，再被高度大的轴向切刀切割后下落的过程中，再被高度低的轴向切刀切割，从而实现对块状物的多次切割，以利于将块状物切割至尺寸较小的碎块。
根据本公开的实施例，上述的径向切刀222具体可以为一体结构，该一体结构在径向方向(在既垂直于导料箱的轴向方向又垂直于固定筒的轴向方向的方向)的两端为切刀结构，该切刀结构为在平行于导料箱的轴向方向上逐渐变薄的结构。以对经由 轴向切刀切割后的块状物进行径向切割。
图12示意性示出了根据本公开第二实施例的固体物料切碎机的结构示意图。
如图12所示，本公开实施例的固体物料切碎机1例如还可以包括物料接收箱60和闸板阀70。物料接收箱60用于接收放置固体物料。该闸板阀70的开关设置于物料接收箱60的外侧，闸板阀70设置于物料接收箱60与导料箱10之间，则通过该闸板阀的开关，可以接通和隔离物料接收箱60与导料箱10。具体地，在需要对固体物料进行切碎磨浆时，可以将装有固体物料的包装袋开口后放入该物料接收箱60。此时将闸板阀70打开，包装袋中的固体物料即可自物料接收箱60中导入导料箱10。
根据本公开的实施例，如图12所示，本公开实施例的固体物料切碎机1中的导料箱10例如可以具有相对设置的一对第三侧壁11，该一对第三侧壁11中的每个第三侧壁11均设置有多个喷嘴111，通过将该喷嘴111与抽液泵及液体箱连接，即可将液体箱中的液体抽入该喷嘴处，并喷入该导料箱10内部。根据本公开的实施例，该一对第三侧壁11上设置的多个喷嘴111具体可以是均匀对称设置的，以在该导料箱10的侧壁处均匀对称地导入液体，使得自物料接收箱60导入的固体物料在该导入的液体的作用下能够沿着导料箱10的轴向方向下落，从而便于固体物料落入相对的一对辊筒之间。此种情况下，料箱中的流动液体可以是由喷嘴导入的液体，而该液体在料箱中的流动可以借助于外力来实现，以将碎块抽运至筛板所在区域。其中，每个第三侧壁11与固定筒的轴向方向及导料箱的轴向方向均平行。
另外，由于自喷嘴111喷入的液体会随着固体物料下落，并流入切碎装置20及料箱30，因此使得本公开实施例的整个固体物料切碎机内部处于液体环境，可以防止在切碎放射性固体废料过程中气溶胶的产生，从而避免对空气的污染。再者，还可以借助于喷嘴导入的液体来实现自助送料，而无需外力作用，因此可以在一定程度上减小整个固体物料切碎机的设备尺寸大小。
图13示意性示出了根据本公开第三实施例的固体物料切碎机的结构示意图。
如图13所示，本公开实施例的固体物料切碎机1为了便于使料箱30中的液体流动，设置了导流泵80。另外，在料箱30与导料箱10的喷嘴111之间例如还可以设置有管道，以使得料箱30中的液体经由该管道流入至喷嘴111处，并喷入导料箱10中，实现料箱30中液体的循环利用。
另外，考虑到料箱30还具有尺寸大于筛板31的筛孔尺寸的较大碎块，此部分较大碎块若直接排出会污染环境。而考虑到料箱30中液体在导流泵80的带动下可以流 动，则该部分较大碎块(即未滤出料箱30的碎块)可以在该流动液体的带动下经由管道流出料箱30，并经由喷嘴111流入至导料箱10中。因此流入该导料箱10的较大碎块可重新被切碎装置切割，直至其尺寸小于筛板31上的筛孔尺寸，被胶体磨40研磨成浆料。
综上可知，本公开实施例通过上述导料泵80的设置，可以实现液体及未研磨废物的回收再利用，并因此提高该固体物料切碎机的处理能力。
本公开的实施例提供了一种反应设备的防护设备及反应***。其中，反应设备的防护装置包括相对设置的一对防护端板以及防护组件。其中，防护组件设置于一对防护端板之间，且该防护组件包括外防护层、内防护层及冷却层。其中，外防护层与一对防护端板围成第一空间。内防护层设置于第一空间内且与一对防护端板围成用于容纳反应设备的第二空间。该内防护层在沿一对防护端板的连线方向上设置有多个导流孔，用于将反应设备的释放物导入外防护层与内防护层之间。冷却层夹设于内防护层与外防护层之间，该冷却层包括能够存储液体的液体管路。其中，防护组件被配置为：在第二空间中容纳有处于工作状态的反应设备的情况下，液体管路中存储有液体，第一空间为封闭空间。
图14示意性示出了根据本公开第一实施例的反应设备的防护装置的结构示意图。
如图14所示，本公开实施例的反应设备14的防护装置1400包括相对设置的一对防护端板1410以及防护组件140。
其中，反应设备14为内部条件能够达到高温高压的设备，例如高温高压炉、反应釜、超临界水反应器等。可以理解的是，此处高温高压的界定标准可以根据实际需求进行界定，也可采用业界公知的标准进行界定，本公开对此不作限定。
其中，防护组件140设置于一对防护端板1410之间。如图14所示，该防护组件140具体可以包括外防护层141、内防护层142及冷却层143。
其中，外防护层141与一对防护端板1410能够围成第一空间。内防护层142设置于该第一空间中，且内防护层142与一对防护端板1410围成第二空间，该第二空间用于容纳反应设备14。冷却层143夹设于内防护层142与外防护层141之间，且该冷却层包括有能够存储液体的液体管路。
根据本公开的实施例，如图14所示，上述内防护层142在沿一对防护端板1410的连线方向上例如还可以设置有多个导流孔。每个导流孔由内防护层142在靠近反应 设备的侧壁及靠近外防护层的侧壁上开设的多个小孔1421连通形成。以在反应设备由于异常而***的情况下，将反应设备的释放物通过该多个导流孔导入外防护层141与内防护层142之间，即将释放物导入冷却层中。根据本公开的实施例，为了保证冷却层不同部分可承受冲击的均衡性，本公开实施例的外防护层141、内防护层142及冷却层143可以同轴设置。
根据本公开的实施例，上述防护组件140具体可以被配置为；在第二空间中容纳有处于工作状态的反应设备14的情况下，冷却层143中的液体管路中存储有液体，且外防护层141与一对相对设置的端板1410之间围成的第一空间为封闭空间。因此，此种情况下，当释放物导入冷却层中时，由于释放物高温高压，而液体管路内部环境为常温常压或低温常压，则由于内外压差的存在，释放物会冲击液体管路，甚至将液体管路冲击破裂。液体管路中的液体可以对释放物降温，而释放物可充斥的空间增大会使得释放物减压。降温减压后的释放物由于外防护层的阻隔，无法释放至防护装置1400外部，而只能存在于第一空间中，因此，当释放物为放射性气体时，可以防止释放物对环境的污染及对人体的损害。
根据本公开的实施例，为了提高降温减压的效率，如图14所示，上述液体管路可以包括多个第一管路1431，该多个第一管路1431在一对防护端板1410的连线方向上延伸设置，且多个第一管路在垂直于内防护层142的方向及内防护层142的周向方向周期排布。通过该多个第一管路1431的设置，可以增加释放物与液体管路的接触面积，从而提高降温效率，且通过该多个第一管路1431，可以存储较多的液体，因此，在释放物冲击破裂第一管路1431时，释放物可充斥的空间明显增大，从而可以快速泄压，防止释放物对外防护层141的冲击损害。
根据本公开的实施例，为了使得反应设备14的释放物能够均匀分散地导入冷却层143，上述内防护层上设置的多个导流孔例如可以在一对防护端板1410的连线方向上周期排布，因此进一步地避免释放物对冷却层的集中冲击。并因此可以增大释放物与冷却层的接触面积，进一步提高降温减压效率。
根据本公开的实施例，上述内防护层与外防护层的厚度及材质具体可以根据实际情况进行设定。例如，内防护层和/或外防护层的主体材质可以包括钢。具体地，内防护层的厚度例如可以为30mm～50mm，其材质例如可以为45号钢等。外防护层的厚度可以为30mm～50mm，其材质例如可以为不锈钢等。
图15A示意性示出了根据本公开实施例的一对防护端板中第一防护端板的结构 示意图；图15B示意性示出根据本公开实施例的一对防护端板中第二防护端板的结构示意图。
根据本公开的实施例，参考图14中一对相对设置的防护端板1410具体可以包括第一防护端板1500和第二防护端板1600。其中，为了向冷却层143的液体管路中导入液体，第一防护端板1500和第二防护端板1600可以分别采用图15A～图15B中的结构。
如图15A所示，本公开实施例的第一防护端板1500可以具有第一液体入口1501、第一液体出口1502，以及连通该第一液体入口1501和第一液体出口1502的第一液体通路1503。
其中，第一液体出口1502与液体管路连通。第一液体入口1501能够在外力作用下打开或关闭，例如，在需要向液体管路中导入液体时该第一液体入口1501处于打开状态，而在不需要导入液体时该第一液体入口1501处于关闭状态。相应地，该第一防护端板1500可以被配置为：在第一液体入口1501打开时，用于使从第一液体入口1501导入的液体流经第一液体通路1503，并使液体自连通的第一液体出口1502流入液体管路，从而实现液体管路中流体的导入。根据本公开的实施例，该第一液体入口1501在导入液体时，具体例如可以与液体存储装置(例如水冷机)等的出液口连通，以将液体存储装置中存储的液体导入。可以理解的是，在需要导出液体时，该第一液体入口1501也可以处于打开状态，且该第一液体入口1501也可以充当出口，只要其于抽液泵连接，且与液体存储装置的进液口连通即可。
根据本公开的实施例，该第一防护端板1500具体例如可以由第一端板1510、第二端板1520和第一筒体1530构成，第一筒体1530位于第一端板1510与第二端板1520之间。且该第一筒体1530的尺寸与第一端板1510及第二端板1520相匹配，或者该第一筒体1530的尺寸小于第一端板1510与第二端板1520的尺寸，以在第一端板1510与第二端板1520之间围成第一液体通路1503，即第一筒体1530的中空部分为第一液体通路1503。此种情况下，第一液体入口1501设置于第一筒体1530上，而第一液体出口1502设置在第一端板1510与第二端板1520中靠近第二防护端板1600的端板上。例如该第一液体出口1502可以设置在第二端板1520上，此时，第二端板1520相对于第一端板1510靠近第二防护端板1600。
根据本公开的实施例，第一端板1510、第二端板1520和第一筒体1530具体例如可以通过焊接等方式形成第一防护端板1500，或者，该第一端板1510、第二端板1520 与第一筒体1530也可以是一体成型形成所述第一防护端板1500的，本公开对此不作限定。
类似的，如图15B所示，本公开实施例的第二防护端板1600可以具有第二液体入口1601、第二液体出口1602，以及连通该第二液体入口1601和第二液体出口1602的第二液体通路1603。
其中，第二液体入口1601与液体管路连通。第二液体出口1602能够在外力作用下打开或关闭，例如，在需要将液体管路中存储的液体导出的情况下，该第二液体出口1602处于打开状态，而在不需要导出液体时该第二液体出口1602处于关闭状态。相应地，该第二防护端板1600可以被配置为：在第二液体出口1602打开时，用于使液体管路中的液体自第二冷却液入口1601流出液体管路，并流经第二液体通路1603后导出第二冷却液出口1602，从而实现液体管路中存储流体的导出。根据本公开的实施例，该第二液体出口1602在导出液体时，具体例如可以与液体存储装置(例如水冷机)等的进液口连通，并在电机等能够提供抽力的设备(例如抽液泵)的带动下，将液体管路中存储的液体导出。可以理解的是，该第二液体出口1602也可以在需要导入液体时处于打开状态，该第二液体出口1602也可以充当入口，只要该第二液体出口1602与液体存储装置的出液口连通，并连接抽液泵即可。
根据本公开的实施例，第二防护端板1600具体例如可以由第三端板1610、第四端板1620和第二筒体1630构成，第二筒体1630位于第三端板1610与第四端板1620之间。且该第二筒体1630的尺寸与第三端板1610及第四端板1620相匹配，或者该第二筒体1630的尺寸小于第三端板1610与第四端板1620的尺寸，以在第三端板1610与第四端板1620之间围成第二液体通路1603，即第二筒体1630的中空部分为第二液体通路1603。此种情况下，第二液体出口1602设置于第二筒体1630上，而第二液体入口1601设置在第三端板1610与第四端板1620中靠近第一防护端板1500的端板上。例如该第二液体入口1601可以设置在第三端板1610上，此时，第三端板1610相对于第四端板1620靠近第一防护端板1500。
根据本公开的实施例，第三端板1610、第四端板1620和第二筒体1630具体例如可以通过焊接等方式形成第二防护端板1600，或者，该第三端板1610、第四端板1620与第二筒体1630也可以是一体成型形成所述第一防护端板1600的，本公开对此不作限定。
根据本公开的实施例，为了保证在该反应设备的防护装置1400中放置有反应设 备的情况下，起到防护作用，防护装置1400应该处于封闭状态。因此该防护装置1400可以被配置为：在第二空间中容纳有处于工作状态的反应设备的情况下，第一液体入口1501与第二液体出口1602关闭，且第一液体通路1503与第二液体通路1603中存储有液体。此种情况下，通过使得第一液体通路1503与第二液体通路1603中存储有液体，可以防止因反应设备的释放物对防护端板的冲击而导致未能完全防护的情况。并因此可以使得在反应设备释放的释放物被完全封闭于该防护装置1400中，避免释放物外泄对环境的污染。
根据本公开的实施例，参考图14中的多个第一管路1431例如可以具有相对设置的第一端和第二端。则该多个第一管路1431可以与两个防护端板连通，以便于液体的导入和导出。具体地，多个第一管路1431的第一端与第一液体出口1502连通，第二端与第二液体入口1601连通。
根据本公开的实施例，上述第一防护端板1500中的第一端板1510、第二端板1520及第一筒体1530的厚度及材质具体可以根据实际需求进行设定。例如，该第一端板1510、第二端板1520和/或第一筒体1530的侧壁的厚度例如可以为30mm～70mm。该第一端板1510、第二端板1520和/或第一筒体1530的主体材质可以为钢，例如可以是不锈钢、45号钢等。
相应地，第二防护端板1600中的第三端板1610、第四端板1620及第二筒体1630的厚度及材质具体可以根据实际需求进行设定。例如，该第三端板1610、第四端板1620和/或第二筒体1630的侧壁的厚度例如可以为30mm～70mm。该第三端板1610、第四端板1620和/或第二筒体1630的主体材质可以为钢，例如可以是不锈钢、45号钢等。
图16示意性示出了根据本公开第二实施例的反应设备的防护装置的结构示意图；图17A示意性示出了参考图16中反应设备的防护装置的正视剖面图；图17B示意性示出了参考图16中反应设备的防护装置的侧视剖面图。
如图16～图17B所示，本公开实施例的反应设备14的防护装置1400与参考图14中的防护装置的区别在于，冷却层143的液体管路除了多个第一管路1431外，还可以包括有多个第二管路1432。
如图16所示，该多个第二管路1432在内防护层142的周向方向上延伸设置，且该多个第二管路1432在一对防护端板的连线方向及垂直于内防护层的方向周期排布。具体地，随着多个第二管路与内防护层距离的增大，在垂直于内防护层的方向上周期排布的第二管路1432的尺寸也逐渐增大。
根据本公开的实施例，该多个第二管路1432的具体尺寸可以根据相对于内防护层相对设置的多对第一管路1431中两个第一管路的距离来确定。以使得该多个第二管路1432中的每个第二管路可以与距离第一内防护层相等距离的一组第一管路1431通过管路连接件连通，从而使得该多个第二管路1432与多个第一管路1431相互连通形成囚笼结构。
相应地，由于第一管路1431的两端分别与两个防护端板的液体通路相连通，因此，本公开实施例的反应设备的防护装置可以被配置为：用于使从第一液体入口1501导入的液体依次流入第一液体通路1503、第一管路1431及第二管路1432。从而可以在导入液体时，使得液体能够流入第一管路1431与第二管路1432，保证该第一管路1431与第二管路1432中均可存储液体。
综上可知，本公开实施例通过上述由第一管路1431与第二管路1432围成的囚笼结构，在释放物导入冷却层143时，可以有效地增大释放物与液体管路的接触面积，并因此释放物可以实现快速的降温减压，释放物会瞬间冷却为液态水，将其彻底消解。且由于外防护层141的阻隔，即使反应器内的释放物全部释放，也不会破坏该防护设备1400，使得释放物能够被很好的限制在外防护层141内部。有效避免对环境的污染。
本公开的另一个方面还提供了一种反应***，该反应***可以包括有反应设备及该反应设备的防护装置。其中，反应设备具体例如可以是高温高压设备，例如可以是超临界水反应设备、高温高压炉或反应釜等。
根据本公开的实施例，反应设备的防护装置可以是参考图14～17B中描述的任意一种防护装置。该防护装置具体包括一对防护端板及防护组件。其中，防护组件包括外防护层、内防护层及冷却层，冷却层夹设于外防护层与内防护层之间。反应设备具体可以放置于由防护装置的内防护层与一对防护端板围成的第二空间中。在此不再赘述。
根据本公开的实施例，由于该反应***不仅具有反应设备，还包括有该反应设备的防护装置，因此可以有效避免反应设备在因意外事故而***的情况下，高温高压的释放物对外界环境的冲击导致的不可预料的事故。根据本公开的实施例，上述反应设备具体可以是超临界水反应设备。
根据本公开的实施例，为了实现核电站及其它核设施的放射性固体可燃物(包括废树脂)的减容减害，本公开提供了一种超临界水氧化***和方法，通过本公开提供 的超临界水氧化***和方法，可以将固体可燃物通过超临界水氧化转化为无机物,同时将有机物中放射性金属元素回收，实现了废物最小化的目的。在实际应用之中，利用该超临界水氧化***和方法处理放射性固体可燃废物的处理能力至少可以达到20kg/h～200kg/h，达到了工程应用规模，纤维织物(工作服、吸水纸、手套、气衣等)减容比可以到达100～150，塑料和橡胶减容比可以达到60～90，废树脂减容比可以达到30～90，废木料减容比可以达到80～120。
本公开实施例提供的超临界水氧化***包括供水装置，用于提供水和目标溶液；氧化剂供料装置，用于为超临界水氧化反应提供氧化剂；固体可燃物切碎磨浆机，用于将固体可燃物磨碎至浆料；超临界水氧化反应器，用于接收固体可燃物磨碎后得到的浆料、氧化剂、水和目标溶液，并提供超临界水氧化反应的反应区；分离设备，用于分离超临界水氧化反应器的流出物。
图18示意性示出了根据本公开实施例的超临界水氧化***的示意图。需要注意的是，图18所示仅为可以应用本公开实施例的超临界水氧化***的示例，以帮助本领域技术人员理解本公开的技术内容，但并不能作为本公开实施例的超临界水氧化***进行不当限定。
如图18所示，超临界水氧化***包括供水装置181、氧化剂供料装置182、固体可燃物切碎磨浆机183、超临界水氧化反应器184和分离设备185。
供水装置181用于提供水和目标溶液。
根据本公开的实施例，供水装置181可以包括用于分别盛装水和目标溶液的多个容器。根据本公开的实施例，目标溶液可以是蔗糖溶液，可以启动蔗糖溶液供料泵，将蔗糖溶液从容器中抽出来。供水装置181还可以包括高压泵，用于将水和目标溶液传输到超临界水氧化反应器184中。
氧化剂供料装置182用于为超临界水氧化反应提供氧化剂。
根据本公开的实施例，氧化剂的种类不做限定。例如，可以是液氧，双氧水等等。氧化剂供料装置182与超临界水氧化反应器184相连，可以将氧化剂输入超临界水氧化反应器184中，以实现超临界水氧化反应。
根据本公开的实施例，以氧化剂为液氧为例，氧化剂供料装置182可以包括杜瓦瓶1821，水浴汽化器1822和高压氧气瓶组1823。液氧可以从杜瓦瓶1821中通过低温高压液氧泵输入水浴汽化器1822，然后从水浴汽化器1822中进入高压氧气瓶组1823。当需要处理固体可燃物时，可以打开单向阀，将氧气从高压氧气瓶组1823中输入超临 界水氧化反应器184中。根据本公开的实施例，液氧设备、管道、阀门及部件材质可以采用超冷低温钢。
固体可燃物切碎磨浆机183用于将固体可燃物磨碎至浆料。
根据本公开的实施例，固体可燃物可以存储在包装箱186中，从包装箱186中将固体可燃物输入固体可燃物切碎磨浆机183中。在启动固体可燃物切碎磨浆机183将固体可燃物磨碎至浆料的过程中，固体可燃物可以先进入大块辊筒阵列切碎，然后进入小块旋转切刀切碎，最后通过控制辊筒转速、旋转切刀转速、导流泵水量进行碎渣胶体磨磨浆，实现放射性固体废物的切碎磨浆。
根据本公开的实施例，固体可燃物切碎磨浆机183可以将固体可燃物磨碎到一定的粒级范围内，例如，可以将固体可燃物磨碎到50μm以下。当需要处理固体可燃物时，可以打开单向阀，将浆料从固体可燃物切碎磨浆机183中输入超临界水氧化反应器184中。根据本公开的实施例，固体可燃物切碎磨浆机183材质可以采用不锈钢。
超临界水氧化反应器184用于接收固体可燃物磨碎后得到的浆料、氧化剂、水和目标溶液，并提供超临界水氧化反应的反应区。
根据本公开的实施例，可以向超临界水氧化反应器184中充入过量的氧化剂，从而保证浆料被充分氧化，根据本公开的实施例，超临界水氧化反应器184的反应温度可以在600℃～800℃之间，压强可以在20Mpa～30Mpa之间。浆料在超临界水氧化反应器184中被充分氧化之后，可以得到氧化产物，通过排料口输送到分离设备185。
分离设备185用于分离超临界水氧化反应器184的流出物。
根据本公开的实施例，分离设备185可以包括活性炭过滤柱1851和高效过滤器1852，设置在分离设备185的排气口处。
根据本公开的实施例，分离设备185的排气口处设置有挥发性有机物在线监测器1853。根据本公开的实施例，分离设备185的蒸发池内配备有液位计(图18中未示出)。根据本公开的实施例，分离设备185的排水口处配备有化学需氧量在线监测器1854。根据本公开的实施例，分离设备185的蒸发池内配备有pH计1855。
根据本公开的实施例，在分离设备185分离流出物的过程中，通过分离设备185上设置的化学需氧量在线监测器1854监测排出的液态物质的COD值；并且/或者通过分离设备185上设置的挥发性有机物在线监测器1853监测排出的气态物质的VOC值；并且/或者通过分离设备185上设置的pH计1855监测分离设备中的蒸发池中溶液的pH值；并且/或者通过分离设备185上设置的温度计监测分离设备中的蒸发池中溶液 的温度和/或冷却内桶内的温度。
根据本公开的实施例，分离设备185还包括背压阀1856，其中，背压阀1856一端通过管道与套管(图18中未示出)连接，背压阀另一端用于通过管道与超临界水氧化反应器184的出料口连接。
根据本公开的实施例，供水装置181、氧化剂供料装置182、固体可燃物切碎磨浆机183、超临界水氧化反应器184和分离设备185设备体积小、能力大、可以实现远距离自动控制，各部分可以为撬装独立单元，以便于总体装备的现场的组合。其中高温高压设备与液氧低温设备可以设计防爆隔离室与泄爆通道等安全防护措施。
图19示意性示出了根据本公开实施例的利用超临界水氧化***处理固体可燃物的方法流程图。
根据本公开的实施例，可以利用超临界水氧化***处理固体可燃物，如图19所示，具体方法可以包括步骤S1901～S1906。
在步骤S1901，将超临界水氧化反应器的腔室温度提升到第一温度。
根据本公开的实施例，例如，可以利用电加热装置预热反应器，使反应器腔室内的温度达到第一温度，例如可以是300℃。
在步骤S1902，通过氧化剂供料装置将氧化剂输入腔室内。
在步骤S1903，通过供水装置将目标溶液输入腔室内，并对腔室继续加热，直到腔室内的温度达到第二温度。
根据本公开的实施例，目标溶液可以是蔗糖溶液，例如，供水装置可以启动蔗糖溶液供料泵，将蔗糖溶液通过超临界水氧化反应器的浆料入口输入腔室内，将反应器温度加热到第二温度，其中，第二温度大于或等于600℃，例如可以是650℃以上。
在步骤S1904，通过固体可燃物切碎磨浆机将固体可燃物磨碎至浆料，并将浆料输入腔室内，以使得浆料与氧化剂发生氧化反应，得到流出物。
根据本公开的实施例，步骤S1901～S1904中的多个步骤可以同时进行。例如，首先启动超临界水氧化反应器的电加热装置，同时启动供水装置中的供水泵，供水装置充满水，泵流量调整到较低状态。超临界水氧化反应器加热升温，直到温度达到300℃之后，启动蔗糖蠕动泵与氧化剂供料装置，用浓蔗糖溶液对超临界水氧化反应器继续加热，直到温度达到600℃以上。例如，超临界水氧化温度保持在650℃至750℃，压力保持在20-25MPa。根据本公开的实施例，固体可燃物切碎磨浆机可以预先将固体可燃物磨碎至浆料，在需要处理浆料时，再将浆料输入腔室内。
在步骤S1905，通过超临界水氧化反应器的出料口将流出物送入分离设备。
根据本公开的实施例，在超临界水氧化反应器停机时，可以先停止进有机物，继续供氧，以便将设备内残留的有机物氧化完毕，之后停止进氧，继续供水，直到水温降到300℃后，停止供水泵，缓缓开启出口背压阀，让超临界水氧化反应器的内部余液缓缓释放到分离设备。
在步骤S1906，通过分离设备分离流出物。
根据本公开的实施例，分离设备185可以将超临界水氧化反应器184的流出物分离为盐渣、蒸馏水和净化气。在固体可燃物为放射性固体可燃物时，可以被氧化成盐溶液和气体，经过分离设备185可以被分离为放射性盐渣、蒸馏水和净化气。放射性盐渣可以过一段时间排渣，大部分蒸馏水可以回流到固体可燃物切碎磨浆机183内循环使用，少量蒸馏水可以收集也可直接排放，净化气体可以收集或直接排放。
根据本公开的实施例，本公开的超临界水氧化***可以用于处理固体可燃物浆料。一般而言，如果固体直接进料超临界水氧化反应器会导致超临界水氧化反应器内堵塞，本公开突破了国内外进料为液体或气体的技术瓶颈，可以将固体经过切碎磨浆后，将浆料的颗粒低于50μm，浆料被泵入超临界水氧化反应器，为防止大颗粒在超临界水反应器内部沉积消除了障碍。
在相关技术中，一般在超临界水氧化反应器内将氧化剂和废料直接进行混合，然后待氧化剂和废料的温度达到一定温度之后才能完全发生反应。但是，由于有机料浆分子量大，分子空间结构稳定，难以在较短的时间内氧化。通过本公开的实施例，当超临界水氧化反应器的腔室内温度达到一定温度时，充入氧化剂，使得可以预先提高氧化剂的温度，再将料浆输入超临界水氧化反应器的腔室内，使得料浆可以进行充分及时热分解，保证了有机料浆进行超临界水氧化的完全性，提高了反应效率。
根据本公开的实施例，采用本公开提供的超临界水氧化***处理固体可燃物的方法包括固体可燃物切碎磨浆、超临界水氧化、流出物自蒸发分离净化，不仅工艺流程短，而且固体可燃物不需要热解预处理，同时，固体有机物直接被超临界水氧化。进一步地，本公开可以比相关技术中的超临界水反应位温度高，反应温度可以达600℃以上，有效提高了反应速率。
下面参考图20～图26，结合具体实施例对图18所示的超临界水氧化***做进一步说明。
图20示意性示出了根据本公开实施例的超临界水氧化反应器的示意图。
如图20所示，超临界水氧化反应器2000包括第一壳体2001，加热装置2002和螺旋环流管2003。
第一壳体2001内部形成用于提供所述反应区的腔室，所述第一壳体2001上至少设置有浆料入口2011、氧化剂入口2012和出料口2013。
根据本公开的实施例，第一壳体2001可以包括外壳和内壳(例如，内壳可以是图20中的内衬2014)，外壳和内壳的形状、材质、尺寸大小不做限定。例如，第一壳体2001的主体部分可以是圆柱型，外壳内径为80～219mm，长度1000～9000mm；内壳内径40～133mm，长度1000～9000mm。
加热装置2002用于提高腔室的温度。根据本公开的实施例，加热装置2002的类型不做限定。例如，加热装置2002可以是加热套。本公开可以将加热套套设在壳体2001的外壁，通过热传导的方式将热量传递给壳体2001内部的腔室，当然本公开也不限定其它加热方式。根据本公开的实施例，超临界水氧化反应器2000的外壳两端可以配备压力表，内壳两端与中间可以配备温度探头，加热套与外壳外壁之间可以配备温度探头。
根据本公开的实施例，加热装置2002可以覆盖第一壳体2001外壁的一部分。例如，加热装置2002可以设置在螺旋环流管2003流出浆料的出口所在的预定区域对应的外壁上，从而覆盖第一壳体2001的一部分。具体地，如图20所示，加热装置2002包括4块加热套，覆盖第一壳体2001的中间至螺旋环流管2003流出浆料的出口的区域。
螺旋环流管2003设置在腔室内，螺旋环流管一端2031与浆料入口2011连通，其中，螺旋环流管2003设置为使得浆料从浆料入口2011导入螺旋环流管2003之后，沿螺旋环流管2003的管道流动，从螺旋环流管另一端流出2032，并与从氧化剂入口2012流入腔室的氧化剂混合并发生氧化反应。
根据本公开的实施例，螺旋环流管2003可以将有机浆料沿着环流管流动，一方面增加有机浆料的流动程度，另一方面增加有机浆料的流速，这样可以增加有机浆料的热解效率。
根据本公开的实施例，螺旋环流管2003可以设置在贴近壳体2001内壁的位置。具体地，在壳体2001包括外壳和内壳的情况下，可以将螺旋环流管2003可以设置在外壳和内壳之间。为了加大有机浆料的流动程度，可以将螺旋环流管2003缠绕内壳进行设置。
根据本公开的实施例，本公开的超临界水氧化反应器2000可以用于处理固体可燃物浆料。通过将固体可燃物切碎磨浆，直接导入螺旋环流管2003中，可以实现在螺旋环流管2003中进行热分解，从螺旋环流管2003流出之后，就可以进行超临界水氧化反应。当超临界水的平均温度为600℃时，有机物热解一般为1秒左右，当有机物流量为30L/h，有机物停留时间最少8s以上，效果好于理论所需。
在相关技术中，如果有机物直接进料，则有机物会冷却反应区温度，减低反应效果。当反应温度为600℃时，有机物热解需要时间为1s左右，当反应温度为550℃时，有机物热解所需时间则为5min，会降低反应效率。可见，本公开相比于现有技术，反应时间非常快，提高了处理效率。
图21示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图。
如图21所示，超临界水氧化反应器2100包括第一壳体2101、加热装置2102、螺旋环流管2103和折返管2104。
其中，第一壳体2101上设置有浆料入口2111、氧化剂入口2112和出料口2113。螺旋环流管2103包括螺旋环流管一端2131和螺旋环流管另一端2132。
需要说明的是，本公开实施例中的第一壳体2101、加热装置2102、螺旋环流管2103可以参考本公开对图20的描述，为了描述的简洁起见，在此不再赘述。
根据本公开的实施例，折返管2104设置在腔室中，折返管2104包括两端开口的内管2141以及一端开口的外管2142，外管2142套设于内管2141的外部，内管2141与氧化剂入口2112连通。
根据本公开的实施例，氧化剂从氧化剂入口2112导入后，经过内管2141，然后进入外管2142，最后从外管2142的一端开口处导出。
根据本公开的实施例，折返管2104可以设置在腔室的中心轴位置。
根据本公开的实施例，内管2141和外管2142的形状、材质、尺寸大小不做限定。例如，内管2141直径可以是φ25～φ42mm，壁厚可以是4～6mm，外管直径可以是42mm以上，壁厚可以是4～6mm，长度都可以在3000mm～6000mm之间。根据本公开的实施例，折返管2104大小适中，可以有效降低生产成本，有利于市场应用。
根据本公开的实施例，折返管可以使得管内氧化剂尽可能升温，增加了预热时间。同时将折返管设置于超临界水反应器中心轴位置，使其受热温度可以达到最高。
根据本公开的实施例，超临界水氧化反应器还包括搅拌器和内衬。
搅拌器包括转轴，转轴穿过第一壳体伸入腔室内，并且/或者转轴穿过出料口伸入 腔室内。内衬设置在腔室中，其中，螺旋环流管沿内衬外壁缠绕设置。该内衬可以相当于超临界水氧化反应器的内壳。
根据本公开的实施例，内衬可以经渗铝、喷丸锻击以及喷涂热障涂层处理，热障涂层包括交替排布的多个铝层和多个氧化铝层。
根据本公开的实施例，内衬经渗铝、喷丸锻击以及喷涂热障涂层处理，热障涂层包括交替排布的多个铝层和多个氧化铝层之后，相当于在内衬上生成了防腐涂层，可以使得通过超临界水的高温作用在内衬的内壁形成一层致密的凝胶层，阻止超临界水与内衬金属的接触与腐蚀。
根据本公开的实施例，形成致密的凝胶层的关键条件是在金属与凝胶层之间有一层致密的特殊金属原子。一方面，这层特殊的金属原子通过金属键与本体金属相连。另一方面又以化学键的形式与凝胶层相连。为了制备这层金属原子，本发明采用镍基金属，首先对金属本体进行渗铝处理，之后用喷丸锻击金属表面，以便形成致密的金属铝原子层，之后喷涂热障涂层，通过金属铝、三氧化二铝陶瓷层的交替喷涂，金属表面形成6～8层的热障涂层，厚度约2～3mm。热障涂层遇到超临界水后，这层热障涂层将转变为致密的凝胶层。凝胶层可以阻止超临界水与内衬金属的接触与腐蚀。
根据本公开的实施例，超临界水氧化反应器还包括冷却装置，设置在侧壁上，用于冷却腔室中产生的反应产物；其中，加热装置与冷却装置可以并排设置在侧壁上，并且，加热装置与第一端壁的距离小于冷却装置与第一端壁的距离。
图22示意性示出了根据本公开另一实施例的超临界水氧化反应器的示意图。
如图22所示，超临界水氧化反应器2200包括第一壳体2201、加热装置2202、螺旋环流管2203、折返管2204、搅拌器2205和冷却装置2206。
其中，第一壳体2201上设置有浆料入口2211、氧化剂入口2212和出料口2213。螺旋环流管2203包括螺旋环流管一端2231和螺旋环流管另一端2232。折返管2204包括两端开口的内管2241以及一端开口的外管2242。搅拌器2205包括转轴2251。根据本公开的实施例，浆料入口2211、氧化剂入口2212和出料口2213的设置位置不做限定。
需要说明的是，本公开实施例中的壳体2201、加热装置2202、螺旋环流管2203和折返管2204等可以参考本公开对图20和图21的描述，为了描述的简洁起见，在此不再赘述。
根据本公开的实施例，如图22所示，搅拌器2205包括转轴2251，转轴2251穿 过壳体2201伸入腔室内，并且/或者转轴2251穿过出料口2213伸入腔室内。
根据本公开的实施例，需要说明的是，搅拌器2205还可以包括转子、隔离套、磁块等等搅拌器所需部件(图22中未示出)。
根据本公开的实施例，第一壳体2201包括第一端壁、侧壁以及与第一端壁相对的第二端壁，其中，浆料入口2211设置在侧壁上，氧化剂入口2212设置在第一端壁上，搅拌器2205和出料口2213设置在第二端壁上，可选地，出料口2213也可以设置在侧壁上。
根据本公开的实施例，搅拌器2205可以是磁力搅拌器，在超临界水氧化反应器2200竖直安装的情况下，可以通过将其安装于超临界水氧化反应器2200的底部，主要用于搅拌反应器底部沉积物，防止出现固体颗粒物沉积、板结、堵塞出料口。
根据本公开的实施例，如图22所示，加热装置2202与第一端壁的距离小于冷却装置2206与第一端壁的距离，也即，加热装置2202更靠近第一端壁，冷却装置2206远离第一端壁。由于浆料和氧化剂在靠近第一端壁的位置发生反应，因此，可以在靠近第一端壁的位置设置加热装置2202，可以在靠近第二端壁的位置设置冷却装置2206。
图23示意性示出了根据本公开实施例的冷却装置506的示意图。
如图23所示，冷却装置2206可以由冷却套组组成，覆盖在超临界水氧化反应器2200的外壁，每个冷却套组包括2个半冷却套2261，2个半冷却套2261可以以固定孔和螺栓2262固定，半冷却套2261中可以充入冷却水，例如按照图22中箭头方式从2个半冷却套2261一端充入水后，然后从2个半冷却套2261另一端排出水。
根据本公开的实施例，需要说明的是，冷却装置2206在冷却腔室中产生的反应产物时，一般不会将反应产物的温度降低到常温，可以是将反应产物的温度降低到比常温高，甚至是高于水沸腾的温度，例如，从500℃降低到300℃。如此设计，由于反应产物排出时的温度较高，不仅减轻了超临界水反应器降温的负担，同时提高超临界水氧化反应器流出物温度后，可以充分利用反应产物自身的温度为后面的反应产物分离设备创造了自发蒸发的必要条件。需要说明的是，冷却装置2206的另一个功能是防止腔室的温度过高，从而防止过热反应。
图24示意性示出了根据本公开实施例的分离设备的示意图。
根据本公开的实施例，分离设备2400包括蒸发池2401和冷却内桶2402。
蒸发池2401用于接收超临界水氧化反应器的流出物，其中，流出物为多态相混合物，其中，蒸发池2401内设置有第一冷却盘管2411和排渣口2412，第一冷却盘管 2411用于在多态相混合物流入蒸发池2401之后，将蒸发池2401中溶液的温度稳定在目标温度范围内，排渣口2412用于排出多态相混合物中的固态物质。
冷却内桶2402，包括第二冷却盘管2421和冷凝水池2422，第二冷却盘管2421用于冷却蒸发池2401中蒸发的蒸汽，冷凝水池2422用于接收第二冷却盘管2421冷却蒸汽后得到的液态物质，冷凝水池2422设置有排水口2423，用于排出液态物质，其中，冷却内桶2402的桶壁上设置有多个孔道，用于供蒸发池2401中蒸发的蒸汽进入冷却内桶2402。
其中，蒸发池2401与冷却内桶2402封装在第二壳体内，蒸发池2401设置在冷却内桶2402下方，第二壳体的顶部设置有排气口2403，用于排放多态相混合物中的气态物质。
根据本公开的实施例，第一冷却盘管2411和第二冷却盘管2421的种类不做限定。例如，可以是螺旋式冷却管。第一冷却盘管2411和第二冷却盘管2421的设置方式不做限定，只要能够实现其对应的功能即可。
根据本公开的实施例，通过将蒸发池2401与冷却内桶2402封装在第二壳体内，实现了固液气多态物质在一体机内分离，省去了冷却设备、气液分离设备、液体冷却设备、气体冷却设备，简化了处理流程。
根据本公开的实施例，蒸发池2401可以接收超临界水反应器的流出物，流出物可以是多态相混合物，蒸发池2401可以将流出物进行蒸发浓缩，然后回收固态物质，蒸汽上升到冷却内桶2402中。
根据本公开的实施例，由于超临界水反应器的流出物可能是高温高压流体，例如反应的流出物本身的温度为150～300℃，压强为25MPa，为了能使高温高压流体平稳蒸发，可以在蒸发池2401中设置冷却盘管，使得流出物可以始终处于沸腾状态。即第一冷却盘管2411将蒸发池2401中溶液的温度稳定在目标温度范围内，例如，可以是在100℃左右，使得溶液可以在蒸发池2401中稳定沸腾。蒸发的蒸汽可以上升到冷却内桶2402中，反应流出物中所包含的例如放射性金属元素可以以无机盐的形式从排渣口2412流出并回收。
根据本公开的实施例，冷凝水池2422蒸发池内设置有用于接收冷凝水池2422多态相混合物的套管，冷凝水池2422套管的管壁上分布有多个小孔，冷凝水池7022多态相混合物通过冷凝水池2422多个小孔分散排入冷凝水池2422蒸发池内。
分离设备2400的排气口2403处设置有挥发性有机物在线监测器2404。根据本公 开的实施例，分离设备2400的排水口2423处配备有化学需氧量在线监测器2405。根据本公开的实施例，分离设备2400的蒸发池2401配备有pH计2406。
根据本公开的实施例，多态相混合物可以是包含固态物质、液体物质和气态物质中的两种以上物质。例如，多态相混合物同时包含固态物质和气态物质，或者同时包含固态物质、液体物质和气态物质。
根据本公开的实施例，多态相混合物可以是有机溶剂蒸残液采用超临界水氧化技术处理后得到的混合物，例如，可以是采用超临界水氧化反应器处理有机溶剂蒸残液后得到的流出物，一般超临界水氧化液体流出物为含盐废水，或者为放射性废水，或者为无机盐水。
在相关技术中，通过超临界水氧化反应器将有机物转化为二氧化碳、水和无机盐之后，一般需要经过冷却设备、气液分离设备、液体冷却设备、气体冷却设备等多个设备处理，才能将二氧化碳、水和无机盐分离。这种处理方式不仅处理流程长，设备多，而且成本高。
通过本公开的实施例，利用分离设备处理多态相混合物，使得多态相混合物中的固态物质在蒸发池底部蒸发浓缩，例如以无机盐渣的形式分离出来；使得多态相混合物中的液态物质在蒸发池中蒸发，经过冷却内桶冷却，可以从冷凝水池的排液口中排出；使得多态相混合物中的气态物质直接可以从分离设备的顶部排出。通过本公开的分离设备，可以同时实现多态相混合物的分离，处理流程不仅短，而且达到了有效降低设备一次性投资和设备运行费用，实现了多态相混合物最大限度减容。
图25示意性示出了根据本公开实施例的冷却内桶的示意图。
如图25所示，冷却内桶2501的桶壁上设置有多个孔道2511，用于供蒸发池中蒸发的蒸汽进入冷却内桶2501。
需要说明的是，本公开实施例中的冷却内桶2501可以参考本公开对图24的描述，为了描述的简洁起见，在此不再赘述。
根据本发明的实施例，可以向冷却内桶2501中的第二冷却盘管2512中充入冷却水，使得冷却内桶2501中的温度相对于蒸发池中的温度低，第二冷却盘管2512充水后可以降低蒸汽的温度。
根据本公开的实施例，例如，蒸发池中蒸发的水蒸汽、氧气和二氧化碳可以从桶壁上设置的多个孔道2511进入冷却内桶2501，如图25中箭头所示的向上流动方向。蒸汽遇到冷空气后，冷凝生成水珠并落入冷凝水池2513中，然后从排液口2514排出。 而氧气和二氧化碳可以从顶部的排气口2515排出。
根据本发明的实施例，冷凝水池2513的体积不做限定。例如，冷凝水池2513的体积可以是50L～500L，冷凝水池2513中可以通过多根辐射管道与外部的环形管道连接，导水能力可以是800kg/h～8000kg/h。冷却盘管2512可以是水平缠绕螺旋冷却管，尺寸大小不做限定。
根据本发明的实施例，桶壁上留有多个孔道2511供气体穿过，冷凝内桶2501能够使得100℃水蒸汽冷凝为60℃～90℃的水，冷凝能力可以是200kg/h～2000kg/h。冷却盘管区的体积不做限定，例如体积可以1000L，冷凝水大部分返回超临界水氧化反应器供水箱中复用，少量可以排放。
图26示意性示出了根据本公开实施例的套管的示意图。
需要说明的是，本公开实施例中的蒸发池2601可以参考本公开对图24～图25的描述，为了描述的简洁起见，在此不再赘述。
如图26所示，蒸发池2601内设置有用于接收多态相混合物的套管2611，套管2611的管壁上分布有多个小孔2612，多态相混合物通过多个小孔2612分散排入蒸发池2601内。
根据本公开的实施例，套管2611的尺寸不做限定。例如，套管2611直径可以φ42～φ50mm，壁厚可以是4～6mm。小孔2612大小不做限定，例如，小孔直径可以是2～3mm，其作用主要是将高速流体通过出口管上的小孔2612得到消解与分散。
根据本公开的实施例，套管2611的种类不做限定。例如，套管2611可以是直管，也可以是螺旋管。
根据本公开的实施例，如图26所示，分离设备还可以包括背压阀2613。背压阀2613一端通过管道与套管2611连接，背压阀2613另一端用于通过管道与超临界水氧化反应器的出料口连接。
根据本公开的实施例，超临界水氧化反应器的流出物通过管道流经背压阀，打开背压阀后，流出物通过套管经过蒸发池时可以以螺旋形式绕行于蒸发池内，将其中的热量传递给处于100℃的水中。之后还可以通过管道从冷却内桶中穿出并与背压阀门相连接，经过减压后又返回到蒸发池内，将其中的气水混合物喷入蒸发池内(100℃，常压)。
根据本公开的实施例，以放射性有机废料为例，氧化产物从超临界水氧化反应器的出料口排出后首先进入蒸发池，在蒸发池内氧化产物依靠自身温度达到蒸发的目的。 经过蒸发后，流出物可以分为三部分：放射性金属盐渣、蒸馏水、净化气体。
根据本公开的实施例，流出物中放射性元素以金属盐的形式作为盐渣间歇排出，蒸发池蒸出的蒸汽在蒸发池上方被冷却以蒸馏水的形式被回收利用，流出物中的氧气与二氧化碳则经过蒸发池水洗、蒸汽冷凝水洗后得到净化。
具体地，以放射性铯和锶为例，放射性铯经过蒸发池蒸发后，去污因子可以达到10 5，水蒸气中的铯不到蒸发池水中铯浓度的十万分之一，蒸发对锶的去污因子可以达到10 9，因此蒸汽可以得到深度净化。
根据本公开的实施例，超临界水氧化反应器的流出物温度比传统流出物温度提高很多。一般地，超临界水氧化反应器的流出物，即氧化产物从出料口排出时，氧化产物从出料口排出时的温度为可以是150℃至300℃之间，而传统流出物温度一般是100℃。采用本公开的分离设备分离氧化产物时，可以使得超临界水反应器排出的氧化产物温度较高，减轻了超临界水反应器降温的负担。在提高超临界水氧化反应器流出物的温度后，为后面的流出物分离设备创造了自发蒸发的必要条件。
本公开的实施例提供了一种超临界水氧化***。该***包括反应器、防护装置、反应器、氧化剂供给装置和有机物供料装置。其中，反应器包括反应器壳体，该反应器壳体上设置有氧化剂进料口、有机物进料口及出料口，该反应器经由出料口排放反应产物。防护装置包括外防护层、冷却层及内防护层，其中，内防护层与外防护层围成有第一空间和第二空间。冷却层包括能够存储液体的液体管路，液体管路设置于第一空间，反应器设置于第二空间，且反应器的出料口延伸至第一空间中除液体管路所在区域之外的区域，使得出料口排放的反应产物能够通过液体管路中存储的液体降温。氧化剂供给装置与氧化剂进料口相连通，有机物供料装置与有机物进料口相连通。
以下参照图27～图28，对本公开实施例提供的超临界水氧化***进行描述。其中，图27示意性示出了根据本公开实施例的超临界水氧化***的结构示意图，图28示意性示出了图27中的A-A剖面图。
如图27所示，本公开实施例的超临界水氧化***2700，包括反应器500、防护装置600、氧化剂供给装置700和有机物供料装置800。其中，氧化剂供给装置700和有机物供料装置800分别用于向反应器500提供氧化剂和有机物。
其中，反应器500包括反应器壳体510，该反应器壳体上设置有有机物进料口501、氧化剂进料口502和出料口503。该反应器500具体可以是超临界水反应器，甚至可 以是超超临界水反应器。
其中，超临界是指温度超过374℃、压力超过22Mpa的状态。而超超临界是指温度达到700℃以上的超临界。在反应器500内条件达到超临界状态时，有机物可以与氧化剂完全混溶。而当超临界温度超过550℃时，有机物中的无机盐的溶解度为零。利用这种性能，可以将有机物(具体例如可以是放射性有机物)转化为二氧化碳、水和无机盐。则利用无机盐在550℃以上溶解度为零的特点实现有机物的分离。上述反应器500具体可以经由出料口排放分离后得到的反应产物。
如图27～28所示，防护装置600包括外防护层610、内防护层620及冷却层630。
其中，冷却层630包括能够存储液体的液体管路631，内防护层620与外防护层610围成有第一空间272和第二空间273。液体管路631设置于第一空间272，反应器500设置于第二空间273中。如图28所示，反应器500的出料口503延伸至第一空间272中除液体管路631所在区域之外的区域，使得出料口503排放的反应产物能够通过液体管路631中存储的液体降温。根据本公开的实施例，该出料口503具体可以延伸至第一空间272中的底部空间，其中，参考图27中反应器500与防护装置600在实际使用时，应该垂直放置，且有机物进料口501处于底部。
其中，氧化剂供给装置700与氧化剂进料口502相连通；以向反应器壳体510包围的空间(反应腔室)提供氧化剂。有机物供料装置800与有机物进料口501相连通，以向反应器壳体510包围的反应腔室提供有机物。
综上可知，上述超临界水氧化***2700通过防护装置600中液体管路631存储的液体，可以对从出料口503喷出的反应产物进行有效降温，并因此得到残渣、冷凝液及废气。因此，上述***2700具有将超临界反应与反应产物冷却分离等功能集成为一体的一体机，在进行超临界水氧化反应时，无需额外设置分离器，并因此有利于超临界水氧化技术的推广应用。
以下参照图27～图29，对本公开实施例提供的防护装置进行描述。其中，图29示意性示出了参考图27中内防护层的结构示意图。
根据本公开的实施例，如图27～28所示，上述外防护层610包括外套筒611和相对设置的一对侧壁端板612。液体管路631具体可以包括多个双层套管。如图28所示，该多个双层套管具体在一对侧壁端板612的连线方向上延伸设置，且该多个双层套管在外套筒611的径向方向及外套筒611的周向方向周期排布。该多个双层套管中每个双层套管都包括有外层套管6311和内层套管6312。
根据本公开的实施例，上述外防护层610中，外套筒611的内径例如可以为
Figure PCTCN2020073313-appb-000001
长度可以为3000～6000mm，其材质具体可以采用钢材质(例如304不锈钢)，其所在环境压力为常压，温度为100℃。起作用主要有两个，一个是接收出料口503排放的反应产物，二是作为反应器的第二道保护屏障。上述双层套管中外层套管尺寸可以为
Figure PCTCN2020073313-appb-000002
内层套管尺寸可以为
Figure PCTCN2020073313-appb-000003
内层管道可承受的压力例如可以为3MPa～5MPa，可承受的温度为600℃。
如图29，内防护层620包括共轴的第一筒体621及相对设置的一对第二筒体622，第一筒体621设置于一对第二筒体622之间，并与一对第二筒体622共轴。其中，第一筒体621包括第一筒体侧壁6211，且该第一筒体621为两端开口的结构。
根据本公开的实施例，如图29所示，一对第二筒体622中每个第二筒体包括第一端板6221和第二筒体侧壁6222。第一端板6221为环形板结构，其内环尺寸与第一筒体621的尺寸相匹配，该一对第二筒体622经由第一端板6221与第一筒体621固定连接。其中，上述第一筒体侧壁6211、第一端板6221及外套筒611围成上述的第一空间272，第一筒体621、第二筒体622及一对侧壁端板612围成第二空间。
根据本公开的实施例，如图29所示，上述第一端板6221上设置有多个第一接口，用于分别与多个双层套管的外层套管6311连通。
根据本公开的实施例，如图29所示，一对第二筒体622中每个第二筒体的第二筒体侧壁6222具有第一开口6222A，其中一个第一开口作为第一进液口，另一个第一开口作为第一出液口。则参考图27～28中的防护装置可以被配置为：在第二空间中设置的反应器处于工作状态时，液体循环地自第一进液口导入，并在流经多个双层套管的外层套管6311后，自第一出液口导出，以对出料口503排放的反应产物进行降温。
根据本公开的实施例，如图29所示，一对第二筒体622中每个第二筒体还包括与第一端板6221相对的第二端板6223、以及设置于第一端板6221和第二端板6223之间的分界板6224。
根据本公开的实施例，上述多个双层套管中每个双层套管的内层套管的长度大于外层套管，且分界板6224上可以设置有多个第二接口6224A，用于分别与多个双层套管的内层套管6312连通。上述第一开口6222A具体则可以设置于第一端板6221与分界板6224之间的第二筒体侧壁6222上。由于第一开口为进液口或出液口，则通过上述设置，可以使得导入第一进液口的液体仅流入外层套管6311，而不会进入内层套管6312。
根据本公开的实施例，如图29所示，第二端板6223上例如可以设置有多个连通孔6223A，用于使内层套管6312与反应器500所在的第二空间273相连通，以形成反应器500的第二道屏障。则在反应器500因意外发生***的情况下，该反应器爆发出的高温高压释放物即可通过该些连通孔6223A流入内层套管6312。此种设计下，外层套管6311通入液体时的功能有两个，一个是冷却出料口503排放的反应产物，二是冷却内层套管在异常情况下导入的释放物。由于内层套管6312与外层套管6311为相互独立、且不连通的两个空间，且内层套管6312通过形成空间273的外套筒与防护装置600外部空间隔离，因此，可以有效避免意外情况的释放物喷出外部空间。
综上可知，本公开实施例的防护装置600即可对正常反应产物进行降温，也可对异常释放物进行降温，在实现产物分离功能的基础上，还兼具防护功能，并因此可以有效避免异常情况高温高压释放物喷出外部空间引起的各种危害。
根据本公开的实施例，上述第二端板6223与分界板6224例如可以为与第一端板6221具有相同尺寸的环形板结构。上述第一筒体及第二筒体的侧壁及端板例如可以由内径
Figure PCTCN2020073313-appb-000004
的厚壁组成，工作可承受的压力为3MPa～5MPa，可承受的温度为600℃。其中，厚壁可以由外皮和主材质构成，外皮可以采用304不锈钢，主材质可以采用45号碳钢。
根据本公开的实施例，如图28所示，冷却层630除了上述多个双层套管外，例如还可以包括冷凝液收集盘632和多个气体管路633。其中，冷凝液收集盘632设置于第一空间272中沿外套筒的径向方向周期排布的相邻两组双层套管之间。其中，所述相邻两组双层套管中，每组双层套管包括有位于同一径向方向的多个双层套管。
根据本公开的实施例，冷凝液收集盘632具体例如可以位于参考图28中靠近出料口503的位置，外防护层610还设置有排液口6112，该排液口6112与冷凝液收集盘632连通。凝液收集盘632在靠近出料口503的第一盘面为封闭结构，且在远离出料口503的第二盘面为开口结构。冷凝液收集盘632具有在外套筒611的轴向方向上周期排列的多个凹槽6321。该多个凹槽6321在垂直于第一盘面和第二盘面的连线方向延伸。上述多个气体管路633沿第一盘面和第二盘面的连线方向上延伸设置于多个凹槽6321处，多个气体管路633在靠近第一盘面的第一端为开口结构，且靠近第二盘面的第二端为闭合结构，且多个气体管路633的第二端高出第二盘面，且多个气体管路633在高出第二盘面的侧壁上具有多个喷气口，以便于出料口排放的反应产物中的蒸汽和不凝性气体混合物能够经由该多个气体管路633传输，并自喷气口喷至冷凝液 收集盘632的第二盘面远离出料口503的一侧。喷至该第二盘面远离出料口503的一侧的蒸汽在外层套管6311中存储的液体的作用下降温形成冷凝液，落入冷凝液收集盘632，并经由排液口6112排出防护装置600。
根据本公开的实施例，如图28所示，外防护层610的外套筒611在冷凝液收集盘632的第二盘面远离出料口503的筒壁还可以设置有排气口6111，以便于不凝性气体排出防护装置600。并且/或者，外防护层610的外套筒611在靠近出料口503的筒壁上还可以设置有排渣口6113，以便于使得出料口503排出的反应产物中的盐渣在重力作用下排出防护装置600。可以理解的是，由于自出料口503排出的反应产物中部分蒸汽可能在蒸发至气体管路之前，已经降温变为冷凝液，因此，在排渣口6113排出盐渣的同时，会有部分的冷凝液排出。
根据本公开的实施例，超临界水氧化***在该排气口6111所在位置处还可以设置有VOC(挥发性有机化合物)在线监测器，在排液口6112所在位置处还可以设置COD(化学需氧量)在线检测器，并在排渣口6113所在位置处设置pH在线监测计，以便于判定反应产物是否会对环境产生危害。
综上可知，本公开实施例通过上述气体管路和冷凝液收集盘的设置，可以有效地实现反应产物的分离，因此可以最大限度的实现有机物的减容。
以下将结合图30～图32B对本公开实施例的反应器500进行描述。其中，图30示意性示出了本公开实施例的反应器的主视截面图，图31示意性示出了参考图30中虚线框区域结构的放大图，图32A示意性示出了参考图31中的B-B剖视左视图，以及图32B示意性示出了参考图31中的B-B剖视右视图。
如图30所示，本公开实施例的反应器500包括的反应器壳体510可以包括第一端壁511、壳体侧壁512以及与第一端壁相对设置的第二端壁513。氧化剂进料口502设置于第一端壁511，出料口503设置于第二端壁，有机物进料口501设置于靠近第二端壁513的壳体侧壁512上。
根据本公开的实施例，上述反应器壳体510采用的材质例如可以为INCONEL625，该壳体侧壁512的内径约为80～219mm，长度约为1000～6000mm。
根据本公开的实施例，该反应器500例如还可以包括有多根有机物输送管520，如图30所示，该多根有机物输送管520沿第一端壁511和第二端壁513的连线方向延伸设置于反应器壳体510内，且该多根有机物输送管520包括第一端及与第一端相对的第二端，其中，靠近有机物进料口501的有机物输送管520的第一端与有机物进料 口501连通。
根据本公开的实施例，如图32A～图32B所示，该多根有机物输送管例如可以在绕反应器500的中心轴的方向上等间距排布，该有机物输送管例如可以为12根、6根、4根等，本公开对该有机物输送管的个数不做限定。如图30～32B所示，该反应器500还可以包括有端部环管530，该端部环管530设置于反应器壳体510内靠近第一端壁511的区域，且端部环管530与多根有机物输送管520的第二端连通，则自有机物输送管的第一端流入的有机物能够流入端部环管530。其中，端部环管530在靠近第二端壁513的侧壁上设置有多个第一出料孔531，并且/或者，多个有机物输送管520在靠近反应器500的中心轴、且靠近第一端壁511的侧壁上设置有多个第二出料孔521，则传输的有机物即可通过该第一出料孔531和/或第二出料孔521均匀的喷入反应器500中靠近第一端壁511的区域的中心(具体可以是中心室)。
根据本公开的实施例，如图30～图32B所示，反应器500还可以包括有第三筒体540及进料板550。其中，第三筒体540套设于多根有机物输送管520及端部环管530的外部。第三筒体540包括第三端板541及第三筒体侧壁542，第三端板541具有与氧化剂进料口502相对应的第一进料孔5411。进料板550设置于第三端板541与端部环管530之间。则在进料板550与第三筒体540之间形成氧化剂传输通道8，且进料板550上设置有多个第二进料孔551。通过上述进料板550和第三筒体540的设置，氧化剂进料口502导入的部分氧化剂通过进料板550上的第二进料孔551可以自反应器500端面喷入中心室，而另一部分氧化剂则通过氧化剂传输通道8传输至有机物输送管520与第三筒体侧壁542之间，并经由相邻两个有机输送管520之间的空隙喷入至中心室。
可以理解的是，该反应器500的内部空间可以根据该第二出料孔521的设置区域，分为参考图30中的两个区域。其中，第一区域51为靠近氧化剂进料口502的区域，该区域中，可通过上述出料孔与进料孔的设置，均匀喷入有氧化剂和有机物，则氧化剂和有机物即可在该第一区域中发生超临界氧化反应。第二区域52为靠近有机物进料口501的区域，该区域中由于没有喷入有机物和氧化剂，且由于该第二区域52靠近出料口503，则第一区域51中反应得到的反应产物即可传输至第二区域52，并经由出料口503排出反应器500。
综上可知，本公开实施例的反应器500，通过上述有机物输送管520、端部环管530、第三筒体540及进料板550的设置，可以使得氧化剂与有机物均能够从反应器 500的端部和侧部均匀的喷入第一区域51的中心。因此可以使得氧化剂与有机物充分接触混合，充分反应，并因此促使反应器第一区域的中心温度达到700～800℃，保证超临界水氧化反应优势的充分发挥。
根据本公开的实施例，反应器500例如还可以包括有内衬560和环流套570。内衬560设置于壳体侧壁512与第三筒体侧壁542之间，环流套570沿内衬560在内衬560与壳体侧壁512之间螺旋缠绕设置在壳体侧壁512上。且上述壳体侧壁512上还设置有第二进液口5121与第二出液口5122。环流套570包括相对的第三端与第四端，第三端与第二进液口5121连通，第四端与第二出液口5122连通。其中，第二进液口5121靠近第二端壁513，第二出液口5122靠近第一端壁511。则自第二进液口5121导入的液体在流经靠近第二端壁513的环流套570时，即可将第二区域52中传输的反应产物的热量传输至靠近第一端壁511的环流套570，实现对喷入的氧化剂及有机物的加热，从而进一步提高有机物与氧化剂的反应温度，保证超临界水氧化反应优势的充分发挥。
根据本公开的实施例，上述内衬560及环流套570例如可以采用GH4169，内衬560的内径例如可以为40～133mm，长度可以为1000～6000mm。环流套570的螺旋外径例如可以接近于壳体侧壁512的内径，螺距为50mm，螺距之间用不锈钢网(例如800目的不锈钢网)填充，从而进一步地增加内衬560的导热面积及液体的停留时间，保证对第二区域52的热量的充分吸收，及对有机物和从侧向喷入的氧化剂的充分加热。使得传输至出料口503的反应产物的温度不至于过高，且有机物和氧化剂的反应温度能够达到超超临界条件。
根据本公开的实施例，为了使得该反应器壳体510内部的温度能够较快的升高，且喷入第一区域51的氧化剂及有机物的温度能够达到超临界条件，上述反应器500还可以包括有加热组件580。该加热组件580设置于第一区域51的外部，用于提升反应器壳体内的温度，并因此对传输的氧化剂和有机物进行加热。根据本公开的实施例，在该反应器500导入有机物与氧化剂之前，例如可以先采用该加热组件580对反应器进行预热，例如可以将反应器预热至300℃。
根据本公开的实施例，为了避免经由出料口503排放的反应产物因温度过高而损害防护装置600，上述反应器500还可以包括冷却组件590。该冷却组件590设置于第二区域52的外部，用于冷却有机物与氧化剂的反应产物。则有机物与氧化剂的反应产物经过环流套570与冷却组件590的双重冷却，可以使得反应产物的温度有效降低， 例如可以降低至120℃～300℃。可以理解的是，经出料口503排放的反应产物的温度也不宜过低，应保证有足够的温度使得反应产物中的水分能够以蒸汽形式蒸发。
根据本公开的实施例，为了避免经由第二区域52的反应产物中的盐渣在靠近第二端壁513的区域因沉积、板结而堵塞出料口503，上述反应器500还可以包括有搅拌组件5100。该搅拌组件5100包括转轴，该转轴穿过反应器壳体及出料口伸入第二区域，则通过该转轴的转动，可以实现对反应物的搅拌，避免对出料口503的堵塞。其中，该搅拌组件5100可以是采用了反应釜标准力搅拌技术的磁力搅拌器，例如可以是型号为CY-2的磁力搅拌器，本公开对此不做限定。
图33示意性示出了本公开实施例的有机物供料装置的结构示意图。
如图33所示，本公开实施例的有机物供料装置800可以包括有第一装置810和第二装置820。
其中，第一装置810包括有机物供料组件811、碱液箱812、第一蠕动泵813、第一高压泵814和第一单向阀815。第一蠕动泵813与碱液箱812连通，第一高压泵814分别与碱液箱812和第一蠕动泵813相连通，第一单向阀815设置于第一高压泵814与有机物进料口501之间。该第一装置810用于提供需要与氧化剂反应的有机物。其中，之所以在有机物中加入碱液，是由于有机物浆料与碱液以一定比例(碱液占有机物重量的30％～100％)混合后被输送到有机物输送管内，可以使得有机物与碱液经过升温，均相溶、碱解，使得有机物深度热解为小分子后自出料孔喷入第一区域51，实现有机物与氧化剂的快速氧化，同时释放大量热量。保证第一区域51的中心温度能够达到超超临界的要求。另外，由于有机物碱解过程为吸热反应，因此在有机物输送管中传输时，有机物碱解可以吸收第一区域***空间热量，从而有效降低靠近反应器壳体510的区域的温度，降低对反应器壳体材料耐高温性能的要求。
其中，第二装置820包括蔗糖溶液箱821、水箱822、第二蠕动泵823、第二高压泵824和第二单向阀825。其中，第二蠕动泵823与蔗糖溶液箱821连通，第二高压泵824分别与水箱822和第二蠕动泵823连通，第二单向阀825设置于第二高压泵824与有机物进料口501之间。
在使用本公开提供的超临界水氧化***进行有机物超临界氧化时，可以先通过参考图30中的加热组件580对反应器500进行预热，在预热至300℃后，将第二装置820与有机物进料口501连通，将蔗糖溶液导入有机物输送管520，由于反应器500预热至了300℃，蔗糖溶液在该300℃环境下，因发生热解而产生大量热量，可对反应器进 一步加热。在将反应器温度加热至650℃后，将第一装置810连通有机物进料口501，向有机物输送管520中导入待氧化的有机物，同时通过氧化剂进料口502导入氧化剂，均匀喷入第一区域51的有机物与氧化剂在650℃环境下瞬间发生超临界水氧化反应，释放大量热量，使得第一区域51的中心区域温度达到700～800℃，达到超超临界条件，则后续喷入的有机物即可与氧化剂发生超超临界水氧化反应，使得有机物完全热解气化，保证超临界水氧化反应优势的充分发挥。
根据本公开的实施例，上述有机物供料组件811具体可以根据需要氧化的有机物的类型选择不同的组件，例如，在有机物为有机废液时，只需要将液体箱作为有机物供料组件811即可。在有机物为固体有机物时，则应该采用能够将固体有机物切碎研磨成浆料的设备作为有机物供料组件811。
根据本公开的实施例，上述氧化剂供给装置700例如可以包括液氧杜瓦瓶、液氧泵、单向阀、液氧汽化器以及高压氧气瓶组，以向反应器500提供氧化剂。
根据本公开的实施例，上述超临界水氧化***例如还可以包括有监测组件，该监测组件包括以下至少一种：设置在反应器壳体510上、出料口503处、冷凝液收集盘632的温度传感器，或设置在反应器壳体510内的压力传感器等。通过该监控组件的设置，可以用于控制氧化物供料的压力和/或流量、有机物供料的压力和/或流量，反应器500的温度和压力。
图34示意性示出了本公开实施例的旋切磨浆机的结构示意图；图35示意性示出了参考图34中旋切磨浆机的俯视图。
在有机物为固体有机物时，例如可以采用参考图34～图35所示的旋切磨浆机811作为有机物供料组件，以将固体有机物切碎研磨成浆料。
如图34～35所示，该旋切磨浆机811包括有相互连通且依次设置的导料箱8111、剪切刀和胶体磨8114。其中，导料箱8111用于导入固体有机物及液体(此处的液体例如可以是自参考图28中的冷凝液收集盘632流出的冷凝液，以实现对液体的回收利用)，导料箱8111的底部设置有导流孔。剪切刀设置于导料箱8111的底部导流孔的上方，用于将下落的固体有机物切成1～5mm的碎渣。胶体磨8114用于将自导流孔流出的碎渣研磨成浆料。其中，剪切刀与胶体磨共轴，以在外力作用下同步转动。
根据本公开的实施例，上述剪切刀包括一级剪切刀8112和二级剪切刀8113，一级剪切刀8112用于将固体有机物切割成10～50mm的碎块，二级剪切刀8113用于将碎块切割成所述1～5mm的碎渣，二级剪切刀8113设置于一级剪切刀8112下方。
根据本公开的实施例，如图34～图35所示，一级剪切刀8112主要由一级旋切刀8112A、一级静止上切刀8112B和一级静止下切刀8112C组成。其中，一级静止上切刀8112B有4把，均匀固定在导料箱8111内壁，位置大约为导料箱8111的下三分之一处，该一级静止上切刀8112B为三角形，三角形顶尖距导料箱8111的侧壁约190mm。一级静止下切刀8112C位于一级静止上切刀8112B的正下方，两者之间的距离刚好容纳一级旋切刀8112A。一级静止下切刀8112C也为三角形，三角形顶尖距导料箱8111的侧壁约为250mm。一级旋切刀8112A主体为窄长条形板，长度约为570mm，宽度约为100mm，厚度约为5mm，在轴心两侧焊接两片向上的刀片，刀片高度约为50mm，距轴心约为100mm，所有刀片均打磨锋利锐角。一级旋切刀8112A的设置目的是在竖向与水平方向对放射性固体废物高速剪切。
根据本公开的实施例，如图34～图35所示，二级剪切刀8113由二级旋切刀8113A与二级静止板8113B组成，二级旋切刀8113A为窄长条形板，长度约为570mm，宽度约为100mm，厚度约为5mm，二级静止板8113B与二级旋切刀8113A距离达到尽可能的小，二级静止板8113B均布分布直径
Figure PCTCN2020073313-appb-000005
的孔，当碎块从孔穿过时被二级旋切刀8113A再一次剪切。二级剪切刀8113剪切得到的碎渣由桶下面的导流孔流入胶体磨8114，在胶体磨8114内进一步研磨至50μm。
综上可知，参考图27～图35描述的超临界水氧化***，有机物超临界水反应的温度能够达到700℃～800℃，解决了难处理废物(例如胺类、阴离子交换树脂等)无法充分氧化的问题。且本公开的超临界水氧化***将有机物氧化、流出物分离及设备防护等功能于一体，为工程应用带来了极大的便利。本公开实施例的超临界水氧化***的处理能力能够达到20～200kg/h，可以满足铀矿提纯、核燃料前处理厂、核燃料制造厂、乏燃料后处理厂等产生的固体可燃物的减容减害需求。
本领域技术人员可以理解，本公开的各个实施例和/或权利要求中记载的特征可以进行多种组合和/或结合，即使这样的组合或结合没有明确记载于本公开中。特别地，在不脱离本公开精神和教导的情况下，本公开的各个实施例和/或权利要求中记载的特征可以进行多种组合和/或结合。所有这些组合和/或结合均落入本公开的范围。
以上对本公开的实施例进行了描述。但是，这些实施例仅仅是为了说明的目的，而并非为了限制本公开的范围。尽管在以上分别描述了各实施例，但是这并不意味着各个实施例中的措施不能有利地结合使用。本公开的范围由所附权利要求及其等同物限定。不脱离本公开的范围，本领域技术人员可以做出多种替代和修改，这些替代和 修改都应落在本公开的范围之内。

Claims (50)

  1. 一种超临界水氧化反应器，包括：
    壳体，内部形成用于提供反应区的腔室，所述壳体上至少设置有浆料入口、氧化剂入口和出料口；
    加热装置，用于提高所述腔室的温度；
    螺旋环流管，设置在所述腔室内，所述螺旋环流管的一端与所述浆料入口连通，其中，浆料从所述浆料入口导入所述螺旋环流管之后，沿所述螺旋环流管的管道流动，并从所述螺旋环流管的另一端流出；
    其中，所述浆料从所述螺旋环流管的另一端流出之后，与从所述氧化剂入口流入所述腔室的氧化剂混合并发生氧化反应。
  2. 根据权利要求1所述的反应器，还包括：
    折返管，设置在所述腔室中，所述折返管包括两端开口的内管以及一端开口的外管，所述外管套设于所述内管的外部，所述内管与所述氧化剂入口连通。
  3. 根据权利要求2所述的反应器，其中，
    所述折返管设置在所述腔室的中心轴位置。
  4. 根据权利要求1所述的反应器，还包括：
    搅拌器，包括转轴，所述转轴穿过所述壳体伸入所述腔室内，并且/或者所述转轴穿过所述出料口伸入所述腔室内。
  5. 根据权利要求4所述的反应器，其中，
    所述壳体包括第一端壁、侧壁以及与所述第一端壁相对的第二端壁，其中，所述浆料入口设置在所述侧壁上，所述氧化剂入口设置在所述第一端壁上，所述搅拌器和所述出料口设置在所述第二端壁上。
  6. 根据权利要求5所述的反应器，还包括：
    内衬，设置在所述腔室中，其中，所述螺旋环流管沿所述内衬外壁缠绕设置，其中，所述内衬经渗铝、喷丸锻击以及喷涂热障涂层处理，所述热障涂层包括交替排布的多个铝层和多个氧化铝层。
  7. 根据权利要求5所述的反应器，还包括：
    冷却装置，设置在所述侧壁上，用于冷却所述腔室中产生的反应产物；其中，所述加热装置与所述冷却装置并排设置在所述侧壁上，并且，所述加热装置与所述第一 端壁的距离小于所述冷却装置与所述第一端壁的距离。
  8. 一种利用权利要求1至7中任一项所述的超临界水氧化反应器处理放射性有机废物的方法，包括：
    通过所述加热装置对所述腔室进行预加热；
    在所述腔室内的温度达到第一温度时，将目标溶液通过所述浆料入口输入所述腔室内，并对所述腔室继续加热，直到所述腔室内的温度达到第二温度；
    将所述放射性有机废物的浆料通过所述浆料入口输入所述螺旋环流管，沿所述螺旋环流管的管道流动，并从所述螺旋环流管的另一端流出；
    在所述放射性有机废物的浆料从所述螺旋环流管的另一端流出之后，与从所述氧化剂入口进入所述腔室的氧化剂混合并发生氧化反应。
  9. 根据权利要求8所述的方法，其中，所述方法还包括：
    在所述超临界水氧化反应器包括折返管的情况下，所述氧化剂先从所述氧化剂入口进入所述折返管，在依次经过所述折返管的内管和外管之后，从所述外管的开口进入所述腔室。
  10. 根据权利要求9所述的方法，其中，所述方法还包括：
    在所述超临界水氧化反应器包括搅拌器的情况下，利用所述搅拌器对发生氧化反应之后得到氧化产物进行搅拌；
    将所述氧化产物从所述出料口排出，其中，所述氧化产物从所述出料口排出时的温度为150℃至300℃之间，所述第二温度大于或等于600℃。
  11. 一种固体物料切碎机，包括相互连通、依次设置的：
    导料箱，用于导入固体物料，并使所述固体物料沿所述导料箱的轴向方向下落；
    切碎装置，包括能够在外力的驱动下转动的切刀，所述切碎装置用于通过所述切刀将沿所述导料箱的轴向方向落入的所述固体物料切成碎块；
    料箱，用于通过导入到所述料箱中的流动液体来带动自所述切碎装置中落入的碎块运动；所述料箱的底部设置有包括多个筛孔的筛板，用于将部分的液体及尺寸小于所述多个筛孔的尺寸的碎块滤出所述料箱；以及
    胶体磨，设置于所述筛板的下方，用于将滤出所述料箱的碎块研磨成浆料。
  12. 根据权利要求11所述的固体物料切碎机，其中，所述切碎装置包括切块组件，所述切块组件包括：
    固定筒，其轴向方向垂直于所述导料箱的轴向方向，且所述固定筒包括第一侧壁， 所述第一侧壁上设置有相对应的第一开口与第二开口，分别用于连通所述导料箱与所述料箱；
    滚动筒，沿所述固定筒的轴向方向设置于所述固定筒内，所述滚动筒包括第二侧壁，所述第二侧壁与所述第一侧壁之间的距离与所述固体物料的尺寸相对应；以及
    多个第一切刀，所述多个第一切刀沿所述滚动筒的周向方向均匀设置于所述第二侧壁的外表面上，形成第一刀阵，用于将沿所述导料箱的轴向方向落入所述第一侧壁与所述第二侧壁之间的固体物料切成块状物，
    其中，所述第一刀阵中两个相邻的第一切刀之间的距离被设置为与所述块状物的尺寸相对应。
  13. 根据权利要求12所述的固体物料切碎机，其中，所述切碎装置还包括：
    粉碎组件，设置于所述固定筒中所述滚动筒与所述料箱之间的位置，所述粉碎组件包括第二切刀，用于将落下的块状物切成所述碎块，
    其中，所述粉碎组件与所述第一侧壁之间的距离大于预设距离，以使所述碎块能够落入所述料箱。
  14. 根据权利要求13所述的固体物料切碎机，其中，所述第二切刀包括轴向切刀和径向切刀，其中：
    所述轴向切刀沿所述导料箱的轴向方向设置；
    所述径向切刀沿与所述导料箱的轴向方向及所述固定筒的轴向方向均垂直的方向设置，所述径向切刀与所述轴向切刀共轴，且所述径向切刀位于所述轴向切刀与所述料箱之间，
    其中，所述轴向切刀和径向切刀被配置为在第一外力的作用下绕共轴的中心轴转动。
  15. 根据权利要求12所述的固体物料切碎机，其中：
    所述切块组件还包括：多个第三切刀，所述多个第三切刀沿所述固定筒的周向方向均匀设置于所述第一侧壁的内表面上，形成第二刀阵；以及
    所述滚动筒能够在所述第二外力的作用下绕其中心轴转动，以使沿所述导料箱的轴向方向落入所述第一侧壁与所述第二侧壁之间的固体物料在所述第一刀阵与所述第二刀阵的作用下被切成所述块状物。
  16. 根据权利要求15所述的固体物料切碎机，其中，所述滚动筒包括：
    至少一组辊筒，每组辊筒包括两个相对的辊筒，所述两个相对的辊筒的侧壁均形 成有所述第一刀阵，且所述两个相对的辊筒能够在所述第二外力的带动下向相反方向转动，
    其中，所述两个相对的辊筒之间的间距小于所述固体物料的尺寸。
  17. 根据权利要求15所述的固体物料切碎机，其中：
    所述多个第一切刀和/或所述多个第二切刀为多棱刀；并且/或者
    所述第一刀阵中相邻两个第一切刀之间的距离和/或所述第二刀阵中相邻两个第三切刀之间的距离为分米量级。
  18. 根据权利要求12所述的固体物料切碎机，其中，所述导料箱包括：
    相对设置的一对第三侧壁，所述一对第三侧壁中的每个第三侧壁均设置有多个喷嘴，用于导入液体，使所述固体物料在所述一对第三侧壁的多个喷嘴导入的液体的作用下沿所述导料箱的轴向方向下落，
    其中，所述每个第三侧壁与所述固定筒的轴向方向及所述导料箱的轴向方向均平行。
  19. 根据权利要求11所述的固体物料切碎机，还包括：
    导流装置，用于驱动导入所述料箱中的流动液体流动，并将未滤出所述料箱的碎块及液体导流至所述导料箱。
  20. 根据权利要求11所述的固体物料切碎机，其中：
    所述碎块在任意一个方向的宽度小于5mm；并且/或者
    所述浆料的颗粒度低于50μm。
  21. 一种反应设备的防护装置，包括：
    相对设置的一对防护端板；以及
    防护组件，设置于所述一对防护端板之间，所述防护组件包括：
    外防护层，与所述一对防护端板围成第一空间；
    内防护层，设置于所述第一空间内且与所述一对防护端板围成用于容纳所述反应设备的第二空间，所述内防护层在沿所述一对防护端板的连线方向上设置有多个导流孔，用于将所述反应设备的释放物导入所述外防护层与内防护层之间；以及
    冷却层，夹设于所述内防护层与外防护层之间，所述冷却层包括能够存储液体的液体管路，
    其中，所述防护组件被配置为：在所述第二空间中容纳有处于工作状态的反应设备的情况下，所述液体管路中存储有液体，所述第一空间为封闭空间。
  22. 根据权利要求21所述的反应设备的防护装置，其中，所述一对防护端板包括第一防护端板和第二防护端板，其中：
    所述第一防护端板具有第一液体入口、第一液体出口及连通所述第一液体入口与所述第一液体出口的第一液体通路，所述第一液体入口在外力作用下能够打开或关闭，所述第一液体出口与所述液体管路连通，所述第一防护端板被配置为：在所述第一液体入口打开时，用于使从所述第一液体入口导入的液体流经所述第一液体通路，并自所述第一液体出口流入所述液体管路；并且/或者
    所述第二防护端板具有第二液体入口、第二液体出口及连通所述第二液体入口与所述第二液体出口的第二液体通路，所述第二液体出口在外力作用下能够打开或关闭，所述第二液体入口与所述液体管路连通，所述第二防护端板被配置为：在所述第二液体出口打开时，用于使所述液体管路中的液体自所述第二冷却液入口流出所述液体管路，并流经所述第二液体通路后导出所述第二冷却液出口，
    其中，所述防护装置被配置为：在所述第二空间中容纳有处于工作状态的反应设备的情况下，所述第一液体入口与所述第二液体出口关闭，且所述第一液体通路与所述第二液体通路中存储有液体。
  23. 根据权利要求21所述的反应设备的防护装置，其中：
    所述一对防护端板中的第一防护端板具有第一液体入口、第一液体出口及连通所述第一液体入口与所述第一液体出口的第一液体通路；
    所述一对防护端板中的第二防护端板具有第二液体入口、第二液体出口及连通所述第二液体入口与所述第二液体出口的第二液体通路；以及
    所述液体管路包括：多个第一管路，在所述一对防护端板的连线方向上延伸设置，且所述多个第一管路在垂直于所述内防护层的方向及所述内防护层的周向方向周期排布，
    其中，所述多个第一管路具有相对设置的第一端和第二端，所述第一端与所述第一液体出口连通，所述第二端与所述第二液体入口连通。
  24. 根据权利要求23所述的反应设备的防护装置，其中，所述液体管路还包括：
    多个第二管路，在所述内防护层的周向方向上延伸设置，且所述多个第二管路在所述一对防护端板的连线方向及垂直于所述内防护层的方向周期排布，
    其中，所述多个第二管路与所述多个第一管路经由多个管路连接件连通，所述防护装置被配置为：用于使从所述第一液体入口导入的液体依次流入所述第一液体通路、 所述第一管路及所述第二管路。
  25. 根据权利要求22所述的反应设备的防护装置，其中：
    所述第一防护端板包括第一端板、第二端板和第一筒体，所述第一筒体设置于所述第一端板和第二端板之间，以在所述第一端板与所述第二端板之间围成所述第一液体通路，所述第一液体入口设置于所述第一筒体上，所述第一液体出口设置于所述第二端板上，且所述第二端板相对于所述第一端板靠近所述第二防护端板；并且/或者
    所述第二防护端板包括第三端板、第四端板和第二筒体，所述第二筒体设置于所述第三端板和第四端板之间，以在所述第三端板与所述第四端板之间围成所述第二液体通路，所述第二液体出口设置于所述第一筒体上，所述第二液体出口设置于所述第三端板上，且所述第三端板相对于所述第四端板靠近所述第一防护端板。
  26. 根据权利要求25所述的反应设备的防护装置，其中：
    所述第一端板和/或所述第二端板的厚度为30mm～70mm，所述第二筒体的高度为30mm～70mm；并且/或者
    所述第三端板和/或所述第四端板的厚度为30mm～70mm，所述第二筒体的高度为30mm～70mm。
  27. 根据权利要求21所述的反应设备的防护装置，其中，所述多个导流孔在所述内防护层上周期排布。
  28. 根据权利要求21所述的反应设备的防护装置，其中：
    所述内防护层的厚度为30mm～50mm；所述外防护层的厚度为30mm～50mm；并且/或者
    所述内防护层和/或所述外防护层的主体材质包括钢。
  29. 一种反应***，包括：
    根据权利要求21～28中任一项所述的反应设备的防护装置；以及
    反应设备，所述反应设备放置于由所述防护装置的内防护层与一对防护端板围成的第二空间中。
  30. 根据权利要求29所述的反应***，其中，所述反应设备包括超临界水反应设备。
  31. 一种超临界水氧化***，包括：
    供水装置，用于提供水和目标溶液；
    氧化剂供料装置，用于为超临界水氧化反应提供氧化剂；
    固体可燃物切碎磨浆机，用于将固体可燃物磨碎至浆料；
    超临界水氧化反应器，用于接收所述固体可燃物磨碎后得到的浆料、所述氧化剂、所述水和所述目标溶液，并提供超临界水氧化反应的反应区；
    分离设备，用于分离所述超临界水氧化反应器的流出物。
  32. 根据权利要求31所述的***，其中，所述超临界水氧化反应器包括：
    第一壳体，内部形成用于提供所述反应区的腔室，所述第一壳体上至少设置有浆料入口、氧化剂入口和出料口；
    加热装置，用于提高所述腔室的温度；
    螺旋环流管，设置在所述腔室内，所述螺旋环流管的一端与所述浆料入口连通，其中，所述螺旋环流管设置为使得所述浆料从所述浆料入口导入所述螺旋环流管之后，沿所述螺旋环流管的管道流动，从所述螺旋环流管的另一端流出，并与从所述氧化剂入口流入所述腔室的氧化剂混合并发生氧化反应。
  33. 根据权利要求32所述的***，所述超临界水氧化反应器还包括：
    折返管，设置在所述腔室中，所述折返管包括两端开口的内管以及一端开口的外管，所述外管套设于所述内管的外部，所述内管与所述氧化剂入口连通。
  34. 根据权利要求33所述的***，其中，
    所述折返管设置在所述腔室的中心轴位置。
  35. 根据权利要求32所述的***，所述超临界水氧化反应器还包括：
    搅拌器，包括转轴，所述转轴穿过所述第一壳体伸入所述腔室内，并且/或者所述转轴穿过所述出料口伸入所述腔室内；
    内衬，设置在所述腔室中，其中，所述螺旋环流管沿所述内衬外壁缠绕设置。
  36. 根据权利要求31所述的***，所述分离设备包括：
    蒸发池，用于接收所述超临界水氧化反应器的流出物，其中，所述流出物为多态相混合物，其中，所述蒸发池内设置有第一冷却盘管和排渣口，所述第一冷却盘管用于在所述多态相混合物流入所述蒸发池之后，将所述蒸发池中溶液的温度稳定在目标温度范围内，所述排渣口用于排出所述多态相混合物中的固态物质；
    冷却内桶，包括第二冷却盘管和冷凝水池，所述第二冷却盘管用于冷却所述蒸发池中蒸发的蒸汽，所述冷凝水池用于接收所述第二冷却盘管冷却所述蒸汽后得到的液态物质，所述冷凝水池设置有排水口，用于排出所述液态物质，其中，所述冷却内桶的桶壁上设置有多个孔道，用于供所述蒸发池中蒸发的蒸汽进入所述冷却内桶；
    其中，所述蒸发池与所述冷却内桶封装在第二壳体内，所述蒸发池设置在所述冷却内桶下方，所述第二壳体的顶部设置有排气口，用于排放所述多态相混合物中的气态物质。
  37. 根据权利要求36所述的***，其中，所述蒸发池内设置有用于接收所述多态相混合物的套管，所述套管的管壁上分布有多个小孔，所述多态相混合物通过所述多个小孔分散排入所述蒸发池内。
  38. 根据权利要求36所述的***，其中，
    所述分离设备还包括背压阀，其中，所述背压阀一端通过管道与所述套管连接，所述背压阀另一端用于通过管道与所述超临界水氧化反应器的出料口连接；并且/或者所述排气口处设置有挥发性有机物在线监测器；并且/或者
    所述蒸发池内配备有液位计；并且/或者
    所述蒸发池内配备有pH计；并且/或者
    所述排水口处配备有化学需氧量在线监测器。
  39. 一种利用权利要求31至38中任一项所述的超临界水氧化***处理固体可燃物的方法，包括：
    将所述超临界水氧化反应器的腔室温度提升到第一温度；
    通过所述氧化剂供料装置将氧化剂输入所述腔室内；
    通过所述供水装置将目标溶液输入所述腔室内，并对所述腔室继续加热，直到所述腔室内的温度达到第二温度；
    通过所述固体可燃物切碎磨浆机将固体可燃物磨碎至浆料，并将所述浆料输入所述腔室内，以使得所述浆料与所述氧化剂发生氧化反应，得到流出物；
    通过所述超临界水氧化反应器的出料口将所述流出物送入所述分离设备；以及
    通过所述分离设备分离所述流出物。
  40. 根据权利要求39所述的方法，其中，在所述分离设备分离所述流出物的过程中，所述方法还包括：
    通过所述分离设备上设置的化学需氧量在线监测器监测排出的液态物质的COD值；并且/或者
    通过所述分离设备上设置的挥发性有机物在线监测器监测排出的气态物质的VOC值；并且/或者
    通过所述分离设备上设置的pH计监测所述分离设备中的蒸发池中溶液的pH值； 并且/或者
    通过所述分离设备上设置的温度计监测所述分离设备中的蒸发池中溶液的温度和/或冷却内桶内的温度。
  41. 一种超临界水氧化***，包括：
    反应器，包括反应器壳体，所述反应器壳体上设置有氧化剂进料口、有机物进料口及出料口，所述反应器经由所述出料口排放反应产物；
    防护装置，包括外防护层、冷却层及内防护层，其中：
    所述内防护层与所述外防护层围成有第一空间和第二空间；
    所述冷却层包括能够存储液体的液体管路，所述液体管路设置于所述第一空间；
    所述反应器设置于所述第二空间，且所述反应器的出料口延伸至所述第一空间中除所述液体管路所在区域之外的区域，使得所述出料口排放的反应产物能够通过所述液体管路中存储的液体降温；
    氧化剂供给装置，与所述氧化剂进料口相连通；以及
    有机物供料装置，与所述有机物进料口相连通。
  42. 根据权利要求41所述的超临界水氧化***，其中：
    所述外防护层包括外套筒和相对设置的一对侧壁端板；
    所述内防护层包括共轴的第一筒体及相对设置的一对第二筒体，所述第一筒体设置于所述一对第二筒体之间，并与所述一对第二筒体共轴，其中：
    所述第一筒体包括第一筒体侧壁，且其为两端开口的结构；
    所述一对第二筒体中每个第二筒体包括第一端板和第二筒体侧壁，所述第一端板为环形板结构，其内环尺寸与所述第一筒体的尺寸相匹配，且所述一对第二筒体经由所述第一端板与所述第一筒体固定连接；
    所述第一筒体侧壁、第一端板及所述外套筒围成所述第一空间，所述第一筒体、第二筒体及所述一对侧壁端板围成所述第二空间；
    所述液体管路包括沿所述一对侧壁端板的连线方向延伸设置的多个双层套管，所述多个双层套管在所述外套筒的径向方向及所述外套筒的周向方向周期排布，且每个双层套管包括外层套管和内层套管，
    其中，所述第一端板上设置有多个第一接口，用于分别与所述多个双层套管的外层套管连通。
  43. 根据权利要求42所述的超临界水氧化***，其中：
    所述一对第二筒体中每个第二筒体的第二侧壁具有第一开口，其中一个第一开口作为第一进液口，另一个第一开口作为第一出液口，
    所述防护装置被配置为：在所述第二空间中设置的反应器处于工作状态时，所述液体循环地自所述第一进液口导入，并在流经所述多个双层套管的外层套管后，自所述第一出液口导出，以对所述出料口排放的反应产物进行降温。
  44. 根据权利要求42所述的超临界水氧化***，其中：
    所述一对第二筒体中每个第二筒体还包括与所述第一端板相对的第二端板、以及设置于所述第一端板和第二端板之间的分界板，所述第一开口设置于所述第一端板与所述分界板之间的侧壁上；
    所述分界板上设置有多个第二接口，用于分别与所述多个双层套管的内层套管连通，所述内层套管的长度大于所述外层套管，所述第二端板上设置有多个连通孔，用于使所述内层套管与所述第二空间相连通，
    其中，所述第二端板及所述分界板为与所述第一端板相同的环形板结构。
  45. 根据权利要求42所述的超临界水氧化***，其中，所述冷却层还包括多个气体管路和冷凝液收集盘，其中：
    所述冷凝液收集盘设置于所述第一空间中沿所述外套筒的径向方向周期排布的相邻两组双层套管之间，所述冷凝液收集盘在靠近所述出料口的第一盘面为封闭结构，且在远离所述出料口的第二盘面为开口结构；所述冷凝液收集盘具有在所述外套筒的轴向方向上周期排列的多个凹槽，且所述多个凹槽在垂直于所述第一盘面和所述第二盘面的连线方向延伸；
    所述多个气体管路沿所述第一盘面和所述第二盘面的连线方向上延伸设置于所述多个凹槽处，所述多个气体管路在靠近所述第一盘面的第一端为开口结构，靠近所述第二盘面的第二端为闭合结构，所述多个气体管路的第二端高出所述第二盘面，且所述多个气体管路在高出所述第二盘面的侧壁上具有多个喷气口，
    其中，外防护层设置有排渣口、排液口及排气口，分别用于排出所述反应产物中的残渣及所述反应产物降温得到冷凝液及废气，所述排液口与所述冷凝液收集盘连通。
  46. 根据权利要求41所述的超临界水氧化***，其中，所述反应器壳体包括第一端壁、壳体侧壁以及与所述第一端壁相对设置的第二端壁，所述氧化剂进料口设置于所述第一端壁，所述出料口设置于所述第二端壁，所述有机物进料口设置于靠近所述第二端壁的壳体侧壁上，所述反应器还包括：
    多根有机物输送管，所述多根有机物输送管沿所述第一端壁和第二端壁的连线方向延伸设置于所述反应器壳体内，所述多根有机物输送管包括第一端及与所述第一端相对的第二端，所述有机物输送管的第一端与所述有机物进料口连通；以及
    端部环管，设置于所述反应器壳体内靠近所述第一端壁的区域，且所述端部环管与所述多根有机物输送管的第二端连通，
    其中，所述端部环管在靠近所述第二端壁的侧壁上设置有多个第一出料孔；并且/或者，所述多个有机物输送管在靠近所述反应器的中心轴、且靠近所述第一端壁的侧壁上设置有多个第二出料孔。
  47. 根据权利要求46所述的超临界水氧化***，其中，所述反应器还包括：
    第三筒体，套设于所述多根有机物输送管及所述端部环管外部，且所述第三筒体包括第三端板及第三筒体侧壁，所述第三端板具有与所述氧化剂进料口相对应的第一进料孔；以及
    进料板，所述进料板设置于所述第三端板与所述端部环管之间，以在所述进料板与所述第三筒体之间形成氧化剂传输通道，且所述进料板上设置有多个第二进料孔。
  48. 根据权利要求47所述的超临界水氧化***，其中：
    所述壳体侧壁上还设置有第二进液口与第二出液口，
    所述反应器还包括：
    内衬，设置于所述壳体侧壁与所述第三筒体侧壁之间；以及
    环流套，沿所述内衬在所述内衬与所述壳体侧壁之间螺旋缠绕设置，且所述环流套包括相对的第三端与第四端，所述第三端与所述第二进液口连通，所述第四端与所述第二出液口连通。
  49. 根据权利要求41所述的超临界水氧化***，其中：
    所述反应器还包括：
    搅拌组件，包括转轴，所述转轴穿过所述反应器壳体及所述出料口；并且/或者所述反应器壳体围成的空间可以分为靠近所述氧化剂进料口的第一区域及靠近所述有机物进料口及所述出料口的第二区域，其中：
    所述反应器还包括：
    加热组件，设置于所述第一区域的外部，用于提升所述反应器壳体内的温度；并且/或者
    冷却组件，设置于所述第二区域的外部，用于冷却氧化剂与有机物的反应产物； 并且/或者
    在所述反应器处于工作状态时，所述第一区域的中心温度为700℃～800℃。
  50. 根据权利要求41所述的超临界水氧化***，其中：
    所述有机物供料装置包括有机物供料组件、碱液箱、第一蠕动泵、第一高压泵和第一单向阀，所述第一蠕动泵与所述碱液箱连通，所述第一高压泵分别与所述碱液箱和所述第一蠕动泵相连通，所述第一单向阀设置于所述第一高压泵与所述有机物进料口之间；以及
    所述有机物供料装置还包括：蔗糖溶液箱、水箱、第二蠕动泵、第二高压泵和第二单向阀，所述第二蠕动泵与所述蔗糖溶液箱连通，所述第二高压泵分别与所述水箱和第二蠕动泵连通，所述第二单向阀设置于所述第二高压泵与所述有机物进料口之间。
PCT/CN2020/073313 2019-02-03 2020-01-20 超临界水氧化处理放射性有机固体废物 WO2020156336A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP20748407.2A EP3919446A4 (en) 2019-02-03 2020-01-20 TREATMENT OF SOLID ORGANIC RADIOACTIVE WASTE BY OXIDATION IN SUPERCRITICAL WATER

Applications Claiming Priority (10)

Application Number Priority Date Filing Date Title
CN201910108862.9 2019-02-03
CN201910108896.8 2019-02-03
CN201910108896.8A CN109772543B (zh) 2019-02-03 2019-02-03 固体物料切碎机
CN201910108898.7 2019-02-03
CN201910109483.1A CN109848182B (zh) 2019-02-03 2019-02-03 超临界水氧化***和处理固体可燃物的方法
CN201910108898.7A CN109647319B (zh) 2019-02-03 2019-02-03 反应设备的防护装置及反应***
CN201910109483.1 2019-02-03
CN201910108890.0 2019-02-03
CN201910108862.9A CN109851029B (zh) 2019-02-03 2019-02-03 超临界水氧化***
CN201910108890.0A CN109851030B (zh) 2019-02-03 2019-02-03 超临界水氧化反应器及处理放射性有机废物的方法

Publications (1)

Publication Number Publication Date
WO2020156336A1 true WO2020156336A1 (zh) 2020-08-06

Family

ID=71841227

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2020/073313 WO2020156336A1 (zh) 2019-02-03 2020-01-20 超临界水氧化处理放射性有机固体废物

Country Status (2)

Country Link
EP (1) EP3919446A4 (zh)
WO (1) WO2020156336A1 (zh)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112047593A (zh) * 2020-08-26 2020-12-08 沈阳理工大学 一种螺旋刮削加药混合催化氧化器及污泥利用方法
CN112844809A (zh) * 2020-12-31 2021-05-28 中铁工程服务有限公司 一种集成化盾构渣土环保处理***
WO2022093945A1 (en) * 2020-10-29 2022-05-05 University Of Washington Hydrothermal reactor systems and methods
CN115739871A (zh) * 2022-10-27 2023-03-07 中核武汉核电运行技术股份有限公司 一种适用于传热管管间沉积泥渣的液动冲击磨削加工装置
CN116444022A (zh) * 2023-05-10 2023-07-18 广东红海湾发电有限公司 一种高含盐高含氯有机废水的超临界水氧化处理***

Citations (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4968009A (en) * 1988-08-27 1990-11-06 Kabushiki Kaisha Kobe Seiko Sho Cooling device for a high temperature, high pressure vessel
JPH11226584A (ja) * 1998-02-17 1999-08-24 Japan Organo Co Ltd 超臨界水酸化方法及び反応装置
US20080135496A1 (en) * 2000-10-10 2008-06-12 Christophe Joussot-Dubien Device for supercritical water oxidation of materials
CN101629028A (zh) * 2009-08-27 2010-01-20 北京科技大学 一种多功能的氧化铝/金属微叠层涂层
WO2013058653A1 (en) * 2011-10-19 2013-04-25 Shredx B.V. Shredding and discharging method for shredding and discharging large-scale household and/or medical waste into a sewer system, and corresponding shredding and discharging device
CN103350103A (zh) * 2013-06-28 2013-10-16 中北大学 超临界水氧化技术处理有机物污染土壤的方法
CN103708599A (zh) * 2012-09-29 2014-04-09 新奥科技发展有限公司 超临界水氧化反应装置和方法
CN105152509A (zh) * 2015-09-10 2015-12-16 新奥科技发展有限公司 超临界反应器、超临界反应***及污泥的超临界处理方法
CN106050416A (zh) * 2015-11-05 2016-10-26 罗浩源 基于超临界二氧化碳的核动力发动机
CN207872358U (zh) * 2017-12-29 2018-09-18 江西海富生物工程有限公司 一种罗汉果高效率连续破碎装置
CN207981332U (zh) * 2018-01-10 2018-10-19 山东润昕生物科技有限公司 透明质酸生产用的物料处理装置
CN109647319A (zh) * 2019-02-03 2019-04-19 中国原子能科学研究院 反应设备的防护装置及反应***
CN109772543A (zh) * 2019-02-03 2019-05-21 中国原子能科学研究院 固体物料切碎机
CN109851029A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化***
CN109851130A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化***和有机废水处理方法
CN109851030A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化反应器及处理放射性有机废物的方法
CN109848182A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化***和处理固体可燃物的方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2891161B1 (fr) * 2005-09-28 2007-11-16 Commissariat Energie Atomique Reacteur et procede pour le traitement en anoxie d'une matiere dans un milieu reactionnel fluide
JP6238116B2 (ja) * 2012-12-04 2017-11-29 株式会社リコー 流体浄化装置
FR3001156B1 (fr) * 2013-01-18 2016-10-21 Commissariat Energie Atomique Dispositif d'oxydation hydrothermale pour le traitement d'une matiere dans un milieu supercritique et procede de mise en oeuvre
CN105782995A (zh) * 2016-05-17 2016-07-20 山东大学 一种超临界水氧化有机物的射流燃烧装置及方法
CN107930538B (zh) * 2017-12-26 2020-02-07 新奥科技发展有限公司 一种超临界水氧化反应器、超临界水氧化***及方法
CN108751383B (zh) * 2018-08-16 2023-11-21 成都九翼环保科技有限公司 逆流式超临界水氧化釜式反应器及其制备方法和用途

Patent Citations (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4968009A (en) * 1988-08-27 1990-11-06 Kabushiki Kaisha Kobe Seiko Sho Cooling device for a high temperature, high pressure vessel
JPH11226584A (ja) * 1998-02-17 1999-08-24 Japan Organo Co Ltd 超臨界水酸化方法及び反応装置
US20080135496A1 (en) * 2000-10-10 2008-06-12 Christophe Joussot-Dubien Device for supercritical water oxidation of materials
CN101629028A (zh) * 2009-08-27 2010-01-20 北京科技大学 一种多功能的氧化铝/金属微叠层涂层
WO2013058653A1 (en) * 2011-10-19 2013-04-25 Shredx B.V. Shredding and discharging method for shredding and discharging large-scale household and/or medical waste into a sewer system, and corresponding shredding and discharging device
CN103708599A (zh) * 2012-09-29 2014-04-09 新奥科技发展有限公司 超临界水氧化反应装置和方法
CN103350103A (zh) * 2013-06-28 2013-10-16 中北大学 超临界水氧化技术处理有机物污染土壤的方法
CN105152509A (zh) * 2015-09-10 2015-12-16 新奥科技发展有限公司 超临界反应器、超临界反应***及污泥的超临界处理方法
CN106050416A (zh) * 2015-11-05 2016-10-26 罗浩源 基于超临界二氧化碳的核动力发动机
CN207872358U (zh) * 2017-12-29 2018-09-18 江西海富生物工程有限公司 一种罗汉果高效率连续破碎装置
CN207981332U (zh) * 2018-01-10 2018-10-19 山东润昕生物科技有限公司 透明质酸生产用的物料处理装置
CN109647319A (zh) * 2019-02-03 2019-04-19 中国原子能科学研究院 反应设备的防护装置及反应***
CN109772543A (zh) * 2019-02-03 2019-05-21 中国原子能科学研究院 固体物料切碎机
CN109851029A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化***
CN109851130A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化***和有机废水处理方法
CN109851030A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化反应器及处理放射性有机废物的方法
CN109848182A (zh) * 2019-02-03 2019-06-07 中国原子能科学研究院 超临界水氧化***和处理固体可燃物的方法

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
CALZAVARA, Y. ET AL.: ""A New Reactor Concept for Hydrothermal Oxidation"", JOURNAL OF SUPERCRITICAL FLUIDS, vol. 31, no. 2, 31 August 2004 (2004-08-31), XP004576497, ISSN: 0896-8446, DOI: 20200413174024Y *
See also references of EP3919446A4 *

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112047593A (zh) * 2020-08-26 2020-12-08 沈阳理工大学 一种螺旋刮削加药混合催化氧化器及污泥利用方法
CN112047593B (zh) * 2020-08-26 2024-01-16 沈阳理工大学 一种螺旋刮削加药混合催化氧化器及污泥利用方法
WO2022093945A1 (en) * 2020-10-29 2022-05-05 University Of Washington Hydrothermal reactor systems and methods
CN112844809A (zh) * 2020-12-31 2021-05-28 中铁工程服务有限公司 一种集成化盾构渣土环保处理***
CN115739871A (zh) * 2022-10-27 2023-03-07 中核武汉核电运行技术股份有限公司 一种适用于传热管管间沉积泥渣的液动冲击磨削加工装置
CN116444022A (zh) * 2023-05-10 2023-07-18 广东红海湾发电有限公司 一种高含盐高含氯有机废水的超临界水氧化处理***
CN116444022B (zh) * 2023-05-10 2023-12-08 广东红海湾发电有限公司 一种高含盐高含氯有机废水的超临界水氧化处理***

Also Published As

Publication number Publication date
EP3919446A4 (en) 2023-01-25
EP3919446A1 (en) 2021-12-08

Similar Documents

Publication Publication Date Title
WO2020156336A1 (zh) 超临界水氧化处理放射性有机固体废物
EP3919448A1 (en) Supercritical water all-in-one machine and organic wastewater treatment method
CN109848182B (zh) 超临界水氧化***和处理固体可燃物的方法
CN109851128B (zh) 超临界水氧化***和废液处理方法
EP3813996B1 (en) Microwave system for converting hydrocarbon-based waste materials into oil and gas fuels
US5424042A (en) Apparatus and method for processing wastes
JP5819607B2 (ja) 減圧熱分解処理装置及び連続油化炭化設備
CN102190363A (zh) 利用辅助燃料补给热量的超临界水氧化反应器
CN101987750B (zh) 废有机物的超临界水处理用预脱盐器
CN109851130B (zh) 超临界水氧化***和有机废水处理方法
RU2394680C2 (ru) Способ и устройство для обработки резиновых отходов
CN109851029B (zh) 超临界水氧化***
CN109851030B (zh) 超临界水氧化反应器及处理放射性有机废物的方法
CN1183053A (zh) 处理有机废料的方法和装置
RU2543619C1 (ru) Устройство для переработки резиновых отходов
RU2422478C1 (ru) Способ переработки органических отходов и устройство для переработки органических отходов
CN109110902A (zh) 一种超临界水氧化***及其启、停控制方法
JP2012148921A (ja) 超微粉炭化物の製造設備
CN210261526U (zh) 一种节能型油泥热解设备
KR102503270B1 (ko) 폐합성고분자 열분해 시스템
CN110546240A (zh) 用于处理煤和生活垃圾的装置
CN109851131B (zh) 超临界水氧化装置和有机废水处理方法
CN102910690A (zh) 一种废水提温和除盐的方法及设备
CN111547981A (zh) 一种处理污油泥装置和***
CN210261523U (zh) 一种安全型油泥热解设备

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20748407

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2020748407

Country of ref document: EP

Effective date: 20210903