CN111161900A - Radioactive organic waste liquid treatment process and system - Google Patents
Radioactive organic waste liquid treatment process and system Download PDFInfo
- Publication number
- CN111161900A CN111161900A CN202010001755.9A CN202010001755A CN111161900A CN 111161900 A CN111161900 A CN 111161900A CN 202010001755 A CN202010001755 A CN 202010001755A CN 111161900 A CN111161900 A CN 111161900A
- Authority
- CN
- China
- Prior art keywords
- pyrolysis furnace
- ash
- flue gas
- liquid
- pyrolysis
- Prior art date
- Legal status (The legal status 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 status listed.)
- Granted
Links
Images
Classifications
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/04—Treating liquids
- G21F9/06—Processing
- G21F9/14—Processing by incineration; by calcination, e.g. desiccation
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/02—Treating gases
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/04—Treating liquids
- G21F9/06—Processing
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/04—Treating liquids
- G21F9/20—Disposal of liquid waste
- G21F9/22—Disposal of liquid waste by storage in a tank or other container
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/28—Treating solids
- G21F9/34—Disposal of solid waste
- G21F9/36—Disposal of solid waste by packaging; by baling
Abstract
The invention provides a radioactive organic waste liquid treatment process and a system, wherein the process comprises the following steps: preparing radioactive organic waste liquid and additives according to a certain proportion and an adding sequence; quantitatively feeding the prepared liquid into a pyrolysis furnace, controlling the temperature of the pyrolysis furnace within a preset range, and performing pyrolysis and neutralization reaction on the prepared liquid to generate pyrolysis ash and organic combustible waste gas; collecting and temporarily storing the pyrolytic ash in an ash discharge hopper, and periodically filling the pyrolytic ash into a waste bucket to be sent into a treatment facility for treatment; filtering the organic combustible waste gas, feeding the organic combustible waste gas into a combustion furnace for combustion, filling the high-temperature flue gas after combustion into a quencher for rapidly cooling to be below a first preset temperature, then reducing the temperature of the flue gas to be below a second preset temperature through a washing tower, and then discharging the flue gas through a tail gas fan. The treatment process and the system of the invention fully separate radioactive substances in the radioactive organic waste liquid, ensure that the inorganic rate of the organic waste liquid after treatment meets the requirements, and effectively solve the problems of environmental pollution and potential safety hazard.
Description
Technical Field
The invention belongs to the technical field of radioactive waste liquid treatment, and particularly relates to a radioactive organic waste liquid treatment process and a radioactive organic waste liquid treatment system.
Background
With the continuous development of the nuclear energy industry, a large amount of spent fuel generated by a nuclear power plant needs to be treated to recycle resources such as unutilized uranium. In the process of recycling uranium resources in spent fuel, a large amount of radioactive organic waste liquid is generated, the main components of the radioactive organic waste liquid are tributyl phosphate (TBP) and kerosene, if the radioactive organic waste liquid is discharged without proper treatment or incomplete treatment, the environment is polluted by radioactivity, the growth of animals and plants is influenced, the water body is deteriorated, the human health is harmed, and the normal operation of the spent fuel treatment process is influenced. If a direct combustion treatment mode is adopted, phosphorus pentoxide is generated in the combustion process of tributyl phosphate, and the phosphorus pentoxide can become phosphoric acid when meeting moisture, so that equipment is seriously corroded, and the discontinuous and stable operation of facilities is caused. In addition, the direct combustion method may cause incomplete combustion due to the problem of liquid phase distribution, the radioactive organic waste liquid cannot be completely inorganic, and the combustion exhaust gas generates pollutants and the like in the cooling treatment process, so that the problems in the radioactive organic waste liquid treatment process need to be solved to ensure the continuous and stable operation of facilities and the standard emission of the exhaust gas.
Disclosure of Invention
The present invention has been made in order to solve, at least in part, the technical problems of incomplete treatment of pollutants, susceptibility to corrosion of equipment, and incomplete mineralization of organic waste liquids, which exist in the prior art.
The technical scheme adopted for solving the technical problem of the invention is as follows:
the invention provides a radioactive organic waste liquid treatment process, which comprises the following steps:
preparing the radioactive organic waste liquid and additives in a suspension preparation tank according to a preset proportion and a preset adding sequence to form a uniform and stable suspension preparation liquid;
quantitatively feeding the prepared liquid in the suspension preparation tank into a pyrolysis furnace, controlling the temperature of the pyrolysis furnace within a preset temperature range, and performing pyrolysis and neutralization reaction on the prepared liquid in the pyrolysis furnace to generate pyrolysis ash and organic combustible waste gas;
collecting the pyrolytic ash and temporarily storing the pyrolytic ash in an ash discharge hopper, loading the pyrolytic ash in the ash discharge hopper into a waste barrel after the preparation liquid is stopped from being supplied for a preset time period when the pyrolysis furnace operates, and then sending the waste barrel into a pyrolytic ash treatment facility; and the number of the first and second groups,
and feeding the organic combustible waste gas into a combustion furnace for combustion, charging high-temperature flue gas generated after combustion into a quencher for rapid cooling to reduce the temperature of the high-temperature flue gas to be below a first preset temperature, washing the rapidly cooled flue gas by a washing tower to reduce the temperature of the flue gas to be below a second preset temperature, and then discharging the washed flue gas by a tail gas fan.
Further, in the preparation process of the preparation solution, the method further comprises the following steps:
stirring the prepared solution, and keeping the stirring speed at 50-250 revolutions per minute; and the number of the first and second groups,
and opening a feeding pump arranged between the suspension preparation tank and the pyrolysis furnace to circulate the preparation liquid so as to ensure that the preparation liquid does not precipitate and separate.
Further, the treatment process further comprises the following steps: placing a steel ball in the pyrolysis furnace, stirring the steel ball and the prepared liquid in the pyrolysis furnace together, controlling the stirring speed to be 1-3 revolutions per minute, enabling the prepared liquid entering the pyrolysis furnace to be uniformly distributed on the surface of the steel ball so as to uniformly heat the prepared liquid, and grinding the generated pyrolysis ash by using the steel ball.
Further, the treatment process further comprises the following steps: filling nitrogen into the pyrolysis furnace in the operation process of the pyrolysis furnace so as to fill the pyrolysis furnace and the ash discharge hopper with the nitrogen; and the number of the first and second groups,
and in the operation process of the pyrolysis furnace, controlling the negative pressure value in the pyrolysis furnace to be stabilized between-1 kPa and-4 kPa by interlocking the output power of the tail gas fan and the negative pressure value in the pyrolysis furnace.
Further, before the preparation liquid in the suspension preparation tank is quantitatively fed into the pyrolysis furnace, the method further comprises the following steps:
starting a tail gas fan to enable the pyrolysis furnace to be at a negative pressure value of-6 kPa to-9 kPa; and the number of the first and second groups,
and (5) carrying out cold leakage inspection on the pyrolysis furnace.
Further, before the organic combustible waste gas is fed into the combustion furnace for combustion, the method further comprises the following steps:
filtering the organic combustible waste gas by a waste gas filtering device; and the number of the first and second groups,
and carrying out back flushing on the waste gas filtering device regularly through nitrogen.
Further, before the pyrolysis ash in the ash discharge hopper is loaded into the waste bucket, the method further comprises the following steps:
controlling the weight of the pyrolytic ash fed into the waste bucket from the ash discharge bucket each time through a pyrolytic ash metering device;
loading the pyrolytic ash in the ash discharge hopper into a waste bin, comprising:
and loading the pyrolytic ash in the ash discharge hopper into a waste bucket through a shielding glove box.
Further, in the combustion process of the organic combustible waste gas, the method further comprises the following steps: and controlling the oxygen content in the combustion furnace to be 8-12% so that the organic combustible waste gas can be completely combusted.
Further, the washing tower comprises a first-stage washing tower and a second-stage washing tower which are connected in series in sequence;
the flue gas after will quick cooling through the scrubbing tower washes so that its temperature reduces to below the second preset temperature, includes:
firstly, introducing the flue gas which is rapidly cooled by a quencher into a primary washing tower, and introducing deionized water into the primary washing tower to wash the flue gas, so that the temperature of the flue gas is reduced to be lower than the preset temperature of underground III; and the number of the first and second groups,
and introducing the flue gas washed by the primary washing tower into a secondary washing tower, and introducing deionized water into the secondary washing tower to wash the flue gas again, so that the temperature of the flue gas is reduced to be lower than a second preset temperature.
Further, the treatment process further comprises the following steps:
further cooling the flue gas washed by the secondary washing tower by using chilled water so as to reduce the content of saturated wet steam in the flue gas; and the number of the first and second groups,
and filtering the flue gas cooled by the chilled water through a flue gas filter, and then discharging the flue gas by a tail gas fan.
Further, in the preparation process of the preparation solution, the method further comprises the following steps:
preparing the additive in an additive preparation tank, and controlling the temperature not to exceed 100 ℃ in the additive preparation process;
temporarily storing the radioactive organic waste liquid in a waste liquid storage tank;
and respectively inputting the additive and the radioactive organic waste liquid into a suspension preparation tank through respective pipelines and pumps arranged on the pipelines for preparation.
According to another aspect of the present invention, there is also provided a radioactive organic waste liquid treatment system comprising: a suspension liquid preparation tank, a pyrolysis furnace, an ash discharge hopper, a waste barrel, a combustion furnace, a quencher, a washing tower and a tail gas fan;
the suspension liquid preparation tank is connected with the pyrolysis furnace through a pipeline; a pyrolysis ash outlet is formed in the bottom of the pyrolysis furnace, and an organic combustible waste gas outlet is formed in the top of the pyrolysis furnace; the pyrolytic ash outlet is sequentially connected with an ash discharge hopper and a waste barrel; the organic combustible waste gas outlet is sequentially connected with a combustion furnace, a quencher, a washing tower and a tail gas fan;
the suspension liquid preparation tank is used for preparing the radioactive organic waste liquid and the additives which are added according to a preset proportion and a preset sequence so as to form a uniform and stable suspension preparation liquid;
the pyrolysis furnace is used for heating and keeping the preparation liquid quantitatively fed into the suspension preparation tank in a preset temperature range, so that the preparation liquid is subjected to pyrolysis and neutralization reaction in the pyrolysis furnace to generate pyrolysis ash and organic combustible waste gas;
the ash discharge hopper is used for collecting and temporarily storing pyrolytic ash generated by the pyrolysis furnace, and after the supply of the preparation liquid is stopped for a preset time length of the operation of the pyrolysis furnace, the pyrolytic ash is loaded into a waste barrel, and the waste barrel is sent into a pyrolytic ash treatment facility for treatment;
the combustion furnace is used for combusting organic combustible waste gas generated by the pyrolysis furnace and charging high-temperature flue gas generated after combustion into the quencher;
the quencher is used for rapidly cooling the high-temperature flue gas generated by the combustion furnace to reduce the temperature of the high-temperature flue gas below a first preset temperature;
the washing tower is used for washing the flue gas which is rapidly cooled by the quencher to reduce the temperature of the flue gas to be below a second preset temperature;
and the tail gas fan is used for discharging the flue gas after washing treatment of the washing tower.
Further, a stirring paddle is arranged in the suspension liquid preparation tank, and is used for stirring the preparation liquid in the preparation process of the preparation liquid, and the stirring speed is kept at 50-250 revolutions per minute;
the processing system further comprises: and the feeding pump is arranged between the suspension preparation tank and the pyrolysis furnace and is used for circulating the preparation liquid so as to ensure that the preparation liquid does not generate precipitation and stratification.
Furthermore, the upper part of the pyrolysis furnace is of a cylindrical structure, the lower part of the pyrolysis furnace is of a conical structure, the cylindrical structure and the conical structure are isolated through an isolation unit, an organic combustible waste gas outlet is formed in the top of the cylindrical structure, and a pyrolysis ash outlet is formed in the bottom of the conical structure;
a stirring paddle is arranged in the cylindrical structure, and a stirring motor is arranged above the pyrolysis furnace to control the stirring paddle to rotate; the inside a plurality of steel balls that still are provided with of column structure, the stirring rake is right with 1 ~ 3 revolutions per minute's stirring speed under agitator motor's control the steel ball with get into the inside preparation liquid of column structure stirs, so that preparation liquid evenly distributed is in the surface of steel ball, it is right preparation liquid carries out the even heating, the steel ball can also be right the pyrolysis ash that produces grinds.
Furthermore, the pyrolysis furnace is also provided with a nitrogen inlet, and nitrogen is filled into the pyrolysis furnace through the nitrogen inlet in the operation process of the pyrolysis furnace, so that the pyrolysis furnace and the ash discharge hopper are filled with nitrogen;
the pyrolysis furnace is also provided with a pressure controller to control the pressure in the pyrolysis furnace, a pressure gauge is arranged in the pressure controller to measure the pressure value in the pyrolysis furnace, the pressure controller is electrically connected with the tail gas fan, and the output power of the tail gas fan is interlocked with the negative pressure value in the pyrolysis furnace to control the negative pressure value in the pyrolysis furnace to be stabilized between-1 kPa and-4 kPa.
Further, the treatment system also comprises a leakage checking device, and the leakage checking device is used for checking cold leakage of the pyrolysis furnace when the tail gas fan is started to enable the pyrolysis furnace to be at a negative pressure value of-6 kPa to-9 kPa.
Furthermore, a waste gas filtering device is arranged at an organic combustible waste gas outlet of the pyrolysis furnace and is used for filtering the organic combustible waste gas generated by the pyrolysis furnace and then charging the filtered organic combustible waste gas into the combustion furnace, and the waste gas filtering device is a sintered ceramic or sintered metal filter;
and a nitrogen back-blowing device is arranged at the top of the waste gas filtering device and is used for regularly back-blowing the waste gas filtering device.
Furthermore, the treatment system also comprises a pyrolytic ash metering device and a shielding glove box;
one end of the pyrolytic ash metering device is connected with the ash discharge hopper, and the other end of the pyrolytic ash metering device is connected with the shielding glove box, so that the weight of pyrolytic ash fed into the waste barrel from the ash discharge hopper every time is controlled through the pyrolytic ash metering device;
the waste barrel is detachably arranged at the bottom of the shielding glove box, so that the pyrolytic ash in the ash discharge hopper is loaded into the waste barrel through the shielding glove box.
Further, an oxygen flow meter is arranged outside the combustion furnace, so that the oxygen content in the combustion furnace is controlled to be 8-12% through the oxygen flow meter, and the organic combustible waste gas can be completely combusted.
Further, the washing tower comprises a first-stage washing tower and a second-stage washing tower which are connected in series in sequence;
one end of the first-stage washing tower is connected with the quencher through a pipeline, and the other end of the first-stage washing tower is connected with the second-stage washing tower through a pipeline; the first-stage washing tower is provided with a first-stage washing circulating pump, and the second-stage washing tower is provided with a second-stage washing circulating pump;
the primary washing circulating pump is used for driving deionized water to circulate so as to wash the flue gas filled into the primary washing tower by the quencher, and the temperature of the flue gas is reduced to be lower than a third preset temperature;
and the secondary washing circulating pump is used for driving deionized water to circulate so as to wash the flue gas filled into the secondary washing tower from the primary washing tower again, and the temperature of the flue gas is reduced to be lower than a second preset temperature.
Furthermore, the treatment system also comprises a tail gas condenser, wherein one end of the tail gas condenser is connected with the secondary washing tower through a pipeline, and the other end of the tail gas condenser is connected with the tail gas fan through a pipeline; the tail gas condenser is used for further cooling the flue gas washed by the secondary washing tower by adopting chilled water so as to reduce the content of saturated wet steam in the flue gas;
the treatment system further comprises a flue gas filter, wherein the flue gas filter is arranged between the tail gas fan and the condenser and used for filtering flue gas cooled by the tail gas condenser, and the filtered flue gas is discharged by the tail gas fan.
Further, the treatment system also comprises a waste liquid storage tank and an additive preparation tank;
the additive preparation tank is also provided with a cooling device, and the cooling device is used for controlling the temperature of the additive preparation tank to be not more than 100 ℃ in the additive preparation process;
the waste liquid storage tank is used for temporarily storing the radioactive organic waste liquid;
the additive preparation tank is communicated with the suspension liquid preparation tank through an additive pump and a pipeline;
the waste liquid storage tank is communicated with the suspension liquid preparation tank through a waste liquid pump and a pipeline.
Has the advantages that:
according to the radioactive organic waste liquid treatment process and system, the radioactive organic waste liquid is pretreated to prepare the stable suspension, strong corrosive phosphoric acid is prevented from being generated in the treatment process, corrosion to equipment such as a pyrolysis furnace is reduced, and the service life of the pyrolysis furnace equipment is greatly prolonged. Be provided with stirring rake and steel ball in the pyrolysis oven, realize thermal transmission through the form of stirring steel ball, evenly distributed is on the steel ball behind the organic waste liquid gets into the pyrolysis oven, avoids leading to the inorganization reaction to be complete inadequately because of the uneven problem of distribution, the unsatisfied problem of requirement of organic waste inorganic rate. The pyrolysis furnace is provided with a plurality of filters, so that pyrolysis ash and radioactive nuclide carried in combustible gas are filtered, the subsequent treatment process of the pyrolysis ash is greatly reduced, and the radioactivity level in equipment in the subsequent process is reduced; the treatment process and the system fully separate and treat radioactive substances in the radioactive organic waste liquid, ensure that the inorganic rate of the organic waste liquid after treatment meets the requirements, and effectively solve the problems of environmental pollution and potential safety hazard; and the treatment process is safe, reliable and efficient, is environment-friendly and has better application prospect.
Drawings
FIG. 1 is a flow chart of a process for treating a radioactive organic waste liquid according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a system for treating a radioactive organic waste liquid according to an embodiment of the present invention.
Detailed Description
In order to make the technical solutions of the present invention better understood, the present invention is further described in detail below with reference to the accompanying drawings and examples.
It should be noted that the embodiments and features of the embodiments of the present invention may be arbitrarily combined with each other without conflict.
In which the terminology used in the embodiments of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the disclosure. As used in the examples of the present invention and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.
As shown in fig. 1, an embodiment of the present invention provides a process for treating a radioactive organic waste liquid, including steps S101 to S104.
Step S101: preparing the radioactive organic waste liquid and additives in a suspension preparation tank according to a preset proportion and a preset adding sequence to form a uniform and stable suspension preparation liquid;
step S102: quantitatively feeding the prepared liquid in the suspension preparation tank into a pyrolysis furnace, controlling the temperature of the pyrolysis furnace within a preset temperature range, and performing pyrolysis and neutralization reaction on the prepared liquid in the pyrolysis furnace to generate pyrolysis ash and organic combustible waste gas;
step S103: collecting the pyrolytic ash and temporarily storing the pyrolytic ash in an ash discharge hopper, loading the pyrolytic ash in the ash discharge hopper into a waste barrel after the preparation liquid is stopped from being supplied for a preset time period when the pyrolysis furnace operates, and then sending the waste barrel into a pyrolytic ash treatment facility; and the number of the first and second groups,
step S104: and feeding the organic combustible waste gas into a combustion furnace for combustion, charging high-temperature flue gas generated after combustion into a quencher for rapid cooling to reduce the temperature of the high-temperature flue gas to be below a first preset temperature, washing the rapidly cooled flue gas by a washing tower to reduce the temperature of the flue gas to be below a second preset temperature, and then discharging the washed flue gas by a tail gas fan.
In the process of recycling uranium resources, a nuclear power plant can generate a large amount of radioactive organic waste liquid, the main components of the radioactive organic waste liquid are tributyl phosphate and kerosene, and a certain additive needs to be added in the treatment process of the radioactive organic waste liquid to enable the tributyl phosphate to react. Generally, different reagents and water are added into a neutralizer preparation tank according to a certain proportion before tributyl phosphate is reacted; in the suspension preparation tank, as for the addition proportion and sequence of the radioactive organic waste liquid and the additive, a person skilled in the art can set the preset proportion and the preset addition sequence according to the actual situation, and add the radioactive liquid, the neutralizer and the additive into the preparation tank at the set rotating speed of the stirring paddle to prepare a stable suspension; concretely, Ca (OH) is added into waste tributyl phosphate-kerosene emulsion according to the proportion2、H2O and a surfactant O-9 (long-chain fatty alcohol-polyoxyethylene ether) are stirred, and the substances are prepared into a uniform, stable and moderate-viscosity suspension emulsion by utilizing the surface activity function of the O-9. Then feeding the raw materials into a pyrolysis furnace, keeping the inside of the pyrolysis furnace in an anoxic state and introducing N2The TBP is pyrolyzed at high temperature. Ca (OH)2Reacting with phosphorus in TBP to generate solid calcium pyrophosphate or calcium phosphate, dropping into an ash hopper below the pyrolysis furnace, mixing combustible gas generated by pyrolysis and unreacted kerosene with hot air, then feeding into a high-temperature combustion furnace for full combustion, and discharging the tail gas after cooling, filtering, leaching and other processes.
The prepared suspension is fed into the pyrolysis furnace in the embodiment of the invention, the preset temperature range is 450-500 ℃, and TBP enters at about 450 ℃ in the inert gas protective atmosphereThermally decomposing to generate gas such as butane and butanone and P2O5，P2O5With Ca (OH) in the feed liquid2Carrying out neutralization reaction to generate Ca2P2O7And (3) a solid. The reaction process is as follows:
2(C4H9O)3PO→P2O5+3C4H10+3C4H8O
P2O5+2Ca(OH)2→Ca2P2O7+2H2O。
in the working process, the prepared suspension emulsion is fed into a pyrolysis furnace through a conveying device, the temperature in the pyrolysis furnace is controlled to be 450-500 ℃, so that the prepared solution is subjected to pyrolysis and neutralization reaction in the pyrolysis furnace, the TBP is heated to perform thermal decomposition reaction, and combustible organic micromolecules and P are generated2O5，P2O5Rapidly react with Ca (OH)2Reacting, completely pyrolyzing the configured liquid before flowing to the bottom of the pyrolysis furnace to generate solid-state slag such as calcium pyrophosphate, dropping the slag into an ash bin at the bottom of the pyrolysis furnace, then entering an ash discharge hopper, entering organic micromolecules into a high-temperature combustion furnace, rapidly cooling the high-temperature flue gas after combustion to a first preset temperature through a quencher, reducing the temperature of the high-temperature flue gas after the high-temperature flue gas is washed to a second preset temperature, and discharging the high-temperature flue gas into the air, wherein the first preset temperature can be 300 ℃, 250 ℃, 200 ℃ and the like, and the second preset temperature can be 50 ℃, 40 ℃, 30 ℃ and the like.
Further, in the preparation process of the preparation solution, the method further comprises the following steps:
stirring the prepared solution, and keeping the stirring speed at 50-250 revolutions per minute; and the number of the first and second groups,
and opening a feeding pump arranged between the suspension preparation tank and the pyrolysis furnace to circulate the preparation liquid so as to ensure that the preparation liquid does not precipitate and separate.
After the suspension liquid is prepared, starting a feeding pump, and starting to circularly stir the prepared suspension liquid without feeding; the organic waste liquid and the additive are fully mixed and kept stable before feeding.
Further, the process also comprises the following steps: placing a steel ball in the pyrolysis furnace, stirring the steel ball and the prepared liquid in the pyrolysis furnace together, controlling the stirring speed to be 1-3 revolutions per minute, enabling the prepared liquid entering the pyrolysis furnace to be uniformly distributed on the surface of the steel ball so as to uniformly heat the prepared liquid, and grinding the generated pyrolysis ash by using the steel ball.
Quantitatively conveying the prepared feed liquid to a pyrolysis furnace, gradually increasing the feeding amount to 5kg/h according to the amount of TBP, calculating the feeding amount of the suspension according to the content of the TBP in the organic waste liquid, and measuring the mass flow of the prepared suspension through a flowmeter, namely the amount of pure TBP is 5kg/h after conversion of the feeding amount. The suspension liquid is subjected to pyrolysis and neutralization reaction in the pyrolysis furnace, pyrolysis ash is obtained at the bottom of the pyrolysis furnace, and combustible gas generated by the reaction enters the combustion furnace for combustion after being filtered by the filter.
And grinding the pyrolytic ash to 100-500 nm through steel balls in a pyrolysis furnace, then feeding the pyrolytic ash into an ash discharge hopper, stopping feeding after a certain amount of pyrolytic ash is accumulated, and maintaining the circulation state of a feeding pump.
The material of the pyrolysis furnace is nickel-based alloy, stainless steel balls with a certain size and uniform size are filled in the pyrolysis furnace, under the action of a stirring paddle, the steel balls move from an outer ring to an inner ring in the pyrolysis furnace, heat of an electric heater on the outer wall of the pyrolysis furnace is brought into the pyrolysis furnace, the steel balls move in a three-dimensional mode under the action of a stirrer, the preparation liquid flows downwards under the action of gravity, the preparation liquid uniformly and stably falls onto the surface of the steel balls, the radioactive organic waste liquid firstly reacts with itself and then reacts with a neutralizing agent in a neutralizing mode, and the quantity of the neutralizing agent must ensure that phosphoric acid generated by the reaction of the organic waste liquid can be completely neutralized. The configured liquid flows to the bottom of the steel ball bed layer and is completely pyrolyzed, and the generated slag such as solid calcium pyrophosphate and the like falls downwards under the extrusion of the dead weight and the steel ball bed layer.
Since the pyrolysis reaction is an endothermic reaction, external heat is also required for gasification, and thus the pyrolysis furnace needs to be heated. The experiment adopts electrical heating to stabilize the temperature in the pyrolysis furnace at 450-500 ℃, so that the temperature required by TBP pyrolysis and kerosene gasification can be ensured, and the reaction in the pyrolysis furnace can be stably carried out.
Further, the process also comprises the following steps: filling nitrogen into the pyrolysis furnace in the operation process of the pyrolysis furnace so as to fill the pyrolysis furnace and the ash discharge hopper with the nitrogen; and the number of the first and second groups,
and in the operation process of the pyrolysis furnace, controlling the negative pressure value in the pyrolysis furnace to be stabilized between-1 kPa and-4 kPa by interlocking the output power of the tail gas fan and the negative pressure value in the pyrolysis furnace.
The negative pressure value in the pyrolysis furnace is stabilized between-1 kPa and-4 kPa, the tail gas fan continuously extracts the organic combustible waste gas in the pyrolysis furnace to enter the combustion furnace, and the organic combustible waste gas generated in the pyrolysis furnace can be prevented from being accumulated. The tail gas fan is the frequency conversion fan, and in the pyrolysis oven operation process, the tail gas fan is chain with the interior negative pressure value of pyrolysis oven, influences the internal pressure operation process at the pyrolysis oven, for example: when nitrogen is filled to blow and sweep equipment or a feed liquid conveying pipeline is cleaned, the output power of the tail gas fan can be adjusted along with the nitrogen, and the negative pressure in the pyrolysis furnace is guaranteed to be stable in a certain range.
Further, before the preparation liquid in the suspension preparation tank is quantitatively fed into the pyrolysis furnace, the method further comprises the following steps:
starting a tail gas fan to enable the pyrolysis furnace to be at a negative pressure value of-6 kPa to-9 kPa; and the number of the first and second groups,
and (5) carrying out cold leakage inspection on the pyrolysis furnace.
Nitrogen is generally filled in the pyrolysis furnace for protection, sealing performance check is needed before feeding the pyrolysis furnace, nitrogen atmosphere protection of the pyrolysis furnace is stopped during the sealing performance check, the temperature in the pyrolysis furnace is heated to 450-500 ℃, a tail gas fan is started, the power of the tail gas fan is adjusted, the pyrolysis furnace is under the negative pressure value of-6 kPa to-9 kPa (gauge pressure), cold leakage check is carried out on the pyrolysis furnace, and the sealing performance of the pyrolysis furnace is ensured to meet the requirement;
further, before the organic combustible waste gas is fed into the combustion furnace for combustion, the method further comprises the following steps:
filtering the organic combustible waste gas by a waste gas filtering device; and the number of the first and second groups,
and carrying out back flushing on the waste gas filtering device regularly through nitrogen.
The produced pyrolysis ash contains radioactive elements, and the radioactivity level in the subsequent setting can be reduced by filtering the organic combustible waste gas. At intervals, the back flushing is carried out on the waste gas filtering position through nitrogen, so that the pyrolysis ash can be prevented from entering subsequent equipment through the filter, and the resistance of the filter is reduced.
Further, the treatment process further comprises the following steps: and in the process of collecting the pyrolytic ash, the bottom parts of the pyrolysis furnace and the ash discharge hopper are shaken, so that the ash discharge operation is facilitated.
The pyrolysis ash is ground to 100-500 nm size through the steel ball in the pyrolysis furnace, contains radionuclide in the pyrolysis ash, needs to collect totally, through rapping pyrolysis furnace and unloading bottom of the hopper, can prevent that the pyrolysis ash from remaining and piling up.
Further, before the pyrolysis ash in the ash discharge hopper is loaded into the waste bucket, the method further comprises the following steps:
controlling the weight of the pyrolytic ash fed into the waste bucket from the ash discharge bucket each time through a pyrolytic ash metering device;
loading the pyrolytic ash in the ash discharge hopper into a waste bin, comprising:
and loading the pyrolytic ash in the ash discharge hopper into a waste bucket through a shielding glove box.
The pyrolysis ash is filled into the waste barrel for further treatment through the metering device and the glove box with the shielding function, the metering device can control the amount of the pyrolysis ash waste in the waste barrel to meet the subsequent metering requirement for the pyrolysis ash waste treatment, and the shielding glove box has the shielding function to reduce the irradiation dose applied to operators. When the device is in normal operation, the gate valve is used for isolating the atmosphere between the metering device and the pyrolysis furnace, so that combustible gas is prevented from entering the metering device.
Further, in the combustion process of the organic combustible waste gas, the method further comprises the following steps: and controlling the oxygen content in the combustion furnace to be 8-12% so that the organic combustible waste gas can be completely combusted.
Controlling the oxygen content in combustion tail gas of a combustion furnace to be 8-12%, heating the charged organic combustible waste gas to 800-1100 ℃, enabling the combustible gas to be completely combusted after entering the combustion furnace and become water, carbon dioxide and the like, enabling the temperature of high-temperature flue gas generated after combustion to reach 800-1100 ℃, enabling the high-temperature flue gas to enter a quencher, and simultaneously spraying deionized water into the quencher, so that the temperature of the flue gas is quickly reduced to be below 250 ℃, and avoiding the generation of pollutants; due to the high operating temperatures, both the pyrolysis furnace and the quencher are lined with refractory bricks.
Further, the washing tower comprises a first-stage washing tower and a second-stage washing tower which are connected in series in sequence;
the flue gas after will quick cooling through the scrubbing tower washes so that its temperature reduces to below the second preset temperature, includes:
firstly, introducing the flue gas which is rapidly cooled by a quencher into a primary washing tower, introducing deionized water into the primary washing tower to wash the flue gas, and reducing the temperature of the flue gas to be lower than a third preset temperature; and the number of the first and second groups,
and introducing the flue gas washed by the primary washing tower into a secondary washing tower, and introducing deionized water into the secondary washing tower to wash the flue gas again, so that the temperature of the flue gas is reduced to be lower than a second preset temperature.
In this embodiment, after the quencher is introduced with deionized water to wash the high-temperature flue gas and rapidly cool the high-temperature flue gas, the first-stage washing tower circulates and washes the tail gas through the first-stage washing liquid circulating pump and lowers the temperature of the tail gas, the second-stage washing tower circulates and further washes the tail gas and lowers the temperature of the tail gas through the second-stage washing liquid circulating pump, wherein the third preset temperature is an intermediate temperature between the first preset temperature and the second preset temperature, which can be any temperature between 150 ℃ and 60 ℃, and harmful substances in the high-temperature flue gas can be better washed through multiple washing.
Further, the process also comprises the following steps: further comprising:
further cooling the flue gas washed by the secondary washing tower by using chilled water so as to reduce the content of saturated wet steam in the flue gas; and the number of the first and second groups,
and filtering the flue gas cooled by the chilled water through a flue gas filter, and then discharging the flue gas by a tail gas fan.
The pyrolysis ash and the acid gas carried in the flue gas are washed by the primary washing tower and the secondary washing tower, and then are cooled to below 20 ℃ by the tail gas cooler, condensate generated in the cooling process is recovered, and the flue gas is filtered by the high-efficiency filter and then is discharged by the tail gas fan.
Further, in the preparation process of the preparation solution, the method further comprises the following steps:
preparing the additive in an additive preparation tank, and controlling the temperature not to exceed 100 ℃ in the additive preparation process;
temporarily storing the radioactive organic waste liquid in a waste liquid storage tank;
and respectively inputting the additive and the radioactive organic waste liquid into a suspension preparation tank through respective pipelines and pumps arranged on the pipelines for preparation.
In the embodiment, the additive is prepared in advance in an additive preparation tank, the additive preparation tank is provided with a cooling device, the temperature of feed liquid is ensured not to exceed 100 ℃, and an outlet of the additive preparation tank is communicated with an inlet of the preparation tank through a pump; the radioactive organic waste liquid in the waste liquid storage tank is conveyed to a preparation tank through a pump, and the preparation tank is communicated with the pyrolysis furnace through a feeding pump; the pipelines are all controlled by a control valve; the pipeline all is equipped with the pipeline and washs, avoids the jam of pipeline.
According to another aspect of the present invention, as shown in fig. 2, an embodiment of the present invention further provides a radioactive organic waste liquid treatment system, including: a suspension preparation tank 1, a pyrolysis furnace 3, an ash discharge hopper 4, a waste barrel 7, a combustion furnace 9, a quencher 10, a washing tower 11 and an exhaust fan 13;
the suspension liquid preparation tank 1 is connected with the pyrolysis furnace 3 through a pipeline; a pyrolysis ash outlet is arranged at the bottom of the pyrolysis furnace 3, and an organic combustible waste gas outlet is arranged at the top of the pyrolysis furnace; the pyrolytic ash outlet is sequentially connected with an ash discharge hopper 4 and a waste barrel 7; the organic combustible waste gas outlet is sequentially connected with a combustion furnace 9, a quencher 10, a washing tower 11 and a tail gas fan 13;
the suspension liquid preparation tank 1 is used for preparing radioactive organic waste liquid and additives which are added according to a preset proportion and a preset sequence so as to form a uniform and stable suspension preparation liquid;
the pyrolysis furnace 3 is used for heating and maintaining the preparation liquid quantitatively fed into the suspension preparation tank in a preset temperature range, so that the preparation liquid is subjected to pyrolysis and neutralization reaction in the pyrolysis furnace 3 to generate pyrolysis ash and organic combustible waste gas;
the ash discharge hopper 4 is used for collecting and temporarily storing pyrolytic ash generated by the pyrolysis furnace 3, and after the preparation liquid supply is stopped for a preset time period when the pyrolysis furnace 3 operates, the pyrolytic ash is loaded into the waste barrel 7, and the waste barrel is sent to a pyrolytic ash treatment facility for treatment;
the combustion furnace 9 is used for combusting organic combustible waste gas generated by the pyrolysis furnace 3, and charging high-temperature flue gas generated after combustion into the quencher 10;
the quencher is used for rapidly cooling the high-temperature flue gas generated by the combustion furnace to reduce the temperature of the high-temperature flue gas below a first preset temperature;
the washing tower 11 is used for washing the flue gas rapidly cooled by the quenching device 10 to reduce the temperature of the flue gas to be lower than a second preset temperature;
and the tail gas fan 13 is used for discharging the flue gas washed by the washing tower 11.
Further, a stirring paddle is arranged in the suspension liquid preparation tank 1, and is used for stirring the preparation liquid in the preparation process of the preparation liquid, and the stirring speed is kept at 50-250 rpm;
the processing system further comprises: and a feed pump 2 arranged between the suspension preparation tank 1 and the pyrolysis furnace 3, wherein the feed pump 2 is used for circulating the preparation liquid to ensure that the preparation liquid does not precipitate and separate.
Further, the upper part of the pyrolysis furnace 3 is of a cylindrical structure, the lower part of the pyrolysis furnace is of a conical structure, the cylindrical structure and the conical structure are isolated through an isolation unit, an organic combustible waste gas outlet is formed in the top of the cylindrical structure, and a pyrolysis ash outlet is formed in the bottom of the conical structure;
a stirring paddle is arranged in the cylindrical structure, and a stirring motor is arranged above the pyrolysis furnace to control the stirring paddle to rotate; the steel ball-grinding device is characterized in that a plurality of steel balls are arranged in the cylindrical structure, the stirring paddle is used for stirring the steel balls and the prepared liquid entering the cylindrical structure at a stirring speed of 1-3 revolutions per minute under the control of a stirring motor, so that the prepared liquid is uniformly distributed on the surface of the steel balls and is uniformly heated, and the steel balls can also grind the generated pyrolytic ash.
The isolation unit is shown with a gap through which the stainless steel balls do not pass, but through which the pyrolysis ash can pass and fall to the bottom of the pyrolysis furnace 3.
Further, the pyrolysis furnace 3 is also provided with a nitrogen inlet, and nitrogen is filled into the pyrolysis furnace 3 and the ash discharge hopper 4 through the nitrogen inlet, so that the pyrolysis furnace 3 and the ash discharge hopper 4 are filled with nitrogen;
the pyrolysis furnace 3 is also provided with a pressure controller for controlling the pressure in the pyrolysis furnace, a pressure gauge is arranged in the pressure controller for measuring the pressure value in the pyrolysis furnace, the pressure controller is electrically connected with the tail gas fan 13, and the output power of the tail gas fan 13 is interlocked with the negative pressure value in the pyrolysis furnace 3 to control the negative pressure value in the pyrolysis furnace 3 to be stabilized between-1 kPa and-4 kPa.
Further, the heat treatment system also comprises a leakage checking device which is used for checking the cold leakage of the pyrolysis furnace 3 when the tail gas fan 13 is started to enable the pyrolysis furnace 3 to be at the negative pressure value of-6 kPa to-9 kPa.
Further, a waste gas filtering device 8 is further arranged at an organic combustible waste gas outlet of the pyrolysis furnace 3, and is used for filtering the organic combustible waste gas generated by the pyrolysis furnace 3 and then charging the filtered organic combustible waste gas into a combustion furnace 9, wherein the waste gas filtering device 8 is a sintered ceramic or sintered metal filter;
and a nitrogen back-blowing device is arranged at the top of the waste gas filtering device 8 and is used for regularly back-blowing the waste gas filtering device 8.
Further, the treatment system also comprises a pyrolytic ash metering device 5 and a shielding glove box 6;
one end of the pyrolytic ash metering device 5 is connected with the ash discharge hopper 4, and the other end of the pyrolytic ash metering device is connected with the shielding glove box 6, so that the weight of pyrolytic ash fed into the waste barrel from the ash discharge hopper every time is controlled by the pyrolytic ash metering device;
the waste barrel 7 is detachably arranged at the bottom of the shielding glove box 6; so that the pyrolysis ash in the ash hopper 4 is loaded into the waste bin 7 through the shielded glove box 6.
Between unloading grey fill 4 and pyrolysis ash metering device 5, between pyrolysis ash metering device 5 and the shielding glove box 6, all have the slide valve and cut off, the slide valve between unloading grey fill 4 and the pyrolysis ash metering device 5 can also be used for cutting off the gas of pyrolysis ash metering device 5 and pyrolysis oven 3, from pyrolysis oven 3 to between the waste drum 7, and equipment and pipeline between pyrolysis oven 3 to tail gas fan 13 all need have good sealing performance, and shielding glove box 6 and waste drum 7 can be better the shielding fall the radioactive ray of nuclear element in the pyrolysis ash.
Further, an oxygen flow meter is arranged outside the combustion furnace 9, so that the oxygen content in the combustion furnace 9 is controlled to be 8-12% through the oxygen flow meter, and the organic combustible waste gas can be completely combusted.
Further, the washing tower 11 comprises a first-stage washing tower 111 and a second-stage washing tower 112 which are connected in series in sequence;
one end of the first-stage scrubber 111 is connected to the expander 10 via a pipe, and the other end is connected to the second-stage scrubber 112 via a pipe; the primary washing tower 111 has a primary washing circulation pump, and the secondary washing tower 112 has a secondary washing circulation pump;
the primary washing circulating pump is used for driving deionized water to circulate so as to wash the flue gas filled into the primary washing tower 111 by the quencher 10, and the temperature of the flue gas is reduced to be lower than a third preset temperature;
the second-stage washing circulation pump is used for driving deionized water to circulate so as to wash the flue gas filled into the second-stage washing tower 112 from the first-stage washing tower again, and the temperature of the flue gas is reduced to be lower than a second preset temperature.
Further, the system further comprises a tail gas condenser 12, wherein one end of the tail gas condenser 12 is connected with the secondary washing tower 112 through a pipeline, and the other end of the tail gas condenser 12 is connected with the tail gas fan 13 through a pipeline, so that the tail gas condenser 12 is used for further cooling the flue gas washed by the secondary washing tower 112 by using chilled water to reduce the content of saturated wet steam in the flue gas;
the treatment system further comprises a flue gas filter, wherein the flue gas filter is arranged between the tail gas fan 13 and the condenser and used for filtering flue gas cooled by the tail gas condenser, and the filtered flue gas is discharged by the tail gas fan 13.
The number of the tail gas fans 13 can be multiple, and the PLC controls the on-off of the tail gas fans 13 according to the required power of the tail gas fans 13.
Further, the treatment system also comprises a waste liquid storage tank 14 and an additive preparation tank 15;
the additive preparation tank 15 is also provided with a cooling device, and the cooling device is used for controlling the temperature of the additive preparation tank 15 not to exceed 100 ℃ in the additive preparation process;
the waste liquid storage tank 14 is used for temporarily storing the radioactive organic waste liquid;
the additive preparation tank 15 is communicated with the suspension preparation tank 1 through an additive pump and a pipeline; the waste liquid storage tank 14 is communicated with the suspension preparing tank 1 through a waste liquid pump and a pipeline.
Further, the suspension liquid preparation tank 1 is also provided with a gas outlet, and the gas outlet is connected with the pyrolysis furnace 3 through a pipeline and a valve, so that gas generated during preparation of the suspension liquid preparation is introduced into the pyrolysis furnace 3.
For the embodiment of the present system, since it basically corresponds to the embodiment of the method, the description is simple, and for the relevant points, reference is made to the corresponding process in the foregoing embodiment of the method, and details are not repeated here.
It will be understood that the above embodiments are merely exemplary embodiments taken to illustrate the principles of the present invention, which is not limited thereto. It will be apparent to those skilled in the art that various modifications and improvements can be made without departing from the spirit and substance of the invention, and these modifications and improvements are also considered to be within the scope of the invention.
Claims (22)
1. A radioactive organic waste liquid treatment process is characterized by comprising the following steps:
preparing the radioactive organic waste liquid and additives in a suspension preparation tank according to a preset proportion and a preset adding sequence to form a uniform and stable suspension preparation liquid;
quantitatively feeding the prepared liquid in the suspension preparation tank into a pyrolysis furnace, controlling the temperature of the pyrolysis furnace within a preset temperature range, and performing pyrolysis and neutralization reaction on the prepared liquid in the pyrolysis furnace to generate pyrolysis ash and organic combustible waste gas;
collecting the pyrolytic ash and temporarily storing the pyrolytic ash in an ash discharge hopper, loading the pyrolytic ash in the ash discharge hopper into a waste barrel after the preparation liquid is stopped from being supplied for a preset time period when the pyrolysis furnace operates, and then sending the waste barrel into a pyrolytic ash treatment facility; and the number of the first and second groups,
and feeding the organic combustible waste gas into a combustion furnace for combustion, charging high-temperature flue gas generated after combustion into a quencher for rapid cooling to reduce the temperature of the high-temperature flue gas to be below a first preset temperature, washing the rapidly cooled flue gas by a washing tower to reduce the temperature of the flue gas to be below a second preset temperature, and then discharging the washed flue gas by a tail gas fan.
2. The process according to claim 1, further comprising, during the preparation of the preparation solution:
stirring the prepared solution, and keeping the stirring speed at 50-250 revolutions per minute; and the number of the first and second groups,
and opening a feeding pump arranged between the suspension preparation tank and the pyrolysis furnace to circulate the preparation liquid so as to ensure that the preparation liquid does not precipitate and separate.
3. The process of claim 1, further comprising: placing a steel ball in the pyrolysis furnace, stirring the steel ball and the prepared liquid in the pyrolysis furnace together, controlling the stirring speed to be 1-3 revolutions per minute, enabling the prepared liquid entering the pyrolysis furnace to be uniformly distributed on the surface of the steel ball so as to uniformly heat the prepared liquid, and grinding the generated pyrolysis ash by using the steel ball.
4. The process of claim 1, further comprising:
filling nitrogen into the pyrolysis furnace in the operation process of the pyrolysis furnace so as to fill the pyrolysis furnace and the ash discharge hopper with the nitrogen; and the number of the first and second groups,
and in the operation process of the pyrolysis furnace, controlling the negative pressure value in the pyrolysis furnace to be stabilized between-1 kPa and-4 kPa by interlocking the output power of the tail gas fan and the negative pressure value in the pyrolysis furnace.
5. The process of claim 1, further comprising, prior to dosing the formulation in the suspension formulation tank into the pyrolysis furnace:
starting a tail gas fan to enable the pyrolysis furnace to be at a negative pressure value of-6 kPa to-9 kPa; and the number of the first and second groups,
and (5) carrying out cold leakage inspection on the pyrolysis furnace.
6. The process of claim 1, further comprising, prior to feeding the organic combustible exhaust gas to the furnace for combustion:
filtering the organic combustible waste gas by a waste gas filtering device; and the number of the first and second groups,
and carrying out back flushing on the waste gas filtering device regularly through nitrogen.
7. The process of claim 1, further comprising, prior to loading the pyrolysis ash in the ash hopper into a waste bin:
controlling the weight of the pyrolytic ash fed into the waste bucket from the ash discharge bucket each time through a pyrolytic ash metering device;
loading the pyrolytic ash in the ash discharge hopper into a waste bin, comprising:
and loading the pyrolytic ash in the ash discharge hopper into a waste bucket through a shielding glove box.
8. The process of claim 1, wherein during the combustion of the organic combustible exhaust gas, further comprising: and controlling the oxygen content in the combustion furnace to be 8-12% so that the organic combustible waste gas can be completely combusted.
9. The process according to claim 1, wherein said washing column comprises a primary washing column and a secondary washing column connected in series;
the flue gas after will quick cooling through the scrubbing tower washes so that its temperature reduces to below the second preset temperature, includes:
firstly, introducing the flue gas which is rapidly cooled by a quencher into a primary washing tower, and introducing deionized water into the primary washing tower to wash the flue gas, so that the temperature of the flue gas is reduced to be lower than the preset temperature of underground III; and the number of the first and second groups,
and introducing the flue gas washed by the primary washing tower into a secondary washing tower, and introducing deionized water into the secondary washing tower to wash the flue gas again, so that the temperature of the flue gas is reduced to be lower than a second preset temperature.
10. The process of claim 9, further comprising:
further cooling the flue gas washed by the secondary washing tower by using chilled water so as to reduce the content of saturated wet steam in the flue gas; and the number of the first and second groups,
and filtering the flue gas cooled by the chilled water through a flue gas filter, and then discharging the flue gas by a tail gas fan.
11. The process according to claim 1, further comprising, during the preparation of the preparation solution:
preparing the additive in an additive preparation tank, and controlling the temperature not to exceed 100 ℃ in the additive preparation process;
temporarily storing the radioactive organic waste liquid in a waste liquid storage tank;
and respectively inputting the additive and the radioactive organic waste liquid into a suspension preparation tank through respective pipelines and pumps arranged on the pipelines for preparation.
12. A radioactive organic waste liquid treatment system, comprising: a suspension liquid preparation tank, a pyrolysis furnace, an ash discharge hopper, a waste barrel, a combustion furnace, a quencher, a washing tower and a tail gas fan;
the suspension liquid preparation tank is connected with the pyrolysis furnace through a pipeline; a pyrolysis ash outlet is formed in the bottom of the pyrolysis furnace, and an organic combustible waste gas outlet is formed in the top of the pyrolysis furnace; the pyrolytic ash outlet is sequentially connected with an ash discharge hopper and a waste barrel; the organic combustible waste gas outlet is sequentially connected with a combustion furnace, a quencher, a washing tower and a tail gas fan;
the suspension liquid preparation tank is used for preparing the radioactive organic waste liquid and the additives which are added according to a preset proportion and a preset sequence so as to form a uniform and stable suspension preparation liquid;
the pyrolysis furnace is used for heating and keeping the preparation liquid quantitatively fed into the suspension preparation tank in a preset temperature range, so that the preparation liquid is subjected to pyrolysis and neutralization reaction in the pyrolysis furnace to generate pyrolysis ash and organic combustible waste gas;
the ash discharge hopper is used for collecting and temporarily storing pyrolytic ash generated by the pyrolysis furnace, and after the supply of the preparation liquid is stopped for a preset time length of the operation of the pyrolysis furnace, the pyrolytic ash is loaded into a waste barrel, and the waste barrel is sent into a pyrolytic ash treatment facility for treatment;
the combustion furnace is used for combusting organic combustible waste gas generated by the pyrolysis furnace and charging high-temperature flue gas generated after combustion into the quencher;
the quencher is used for rapidly cooling the high-temperature flue gas generated by the combustion furnace to reduce the temperature of the high-temperature flue gas below a first preset temperature;
the washing tower is used for washing the flue gas which is rapidly cooled by the quencher to reduce the temperature of the flue gas to be below a second preset temperature;
and the tail gas fan is used for discharging the flue gas after washing treatment of the washing tower.
13. The processing system of claim 12,
a stirring paddle is arranged in the suspension liquid preparation tank, and is used for stirring the preparation liquid in the preparation process of the preparation liquid, and the stirring speed is kept at 50-250 revolutions per minute;
the processing system further comprises: and the feeding pump is arranged between the suspension preparation tank and the pyrolysis furnace and is used for circulating the preparation liquid so as to ensure that the preparation liquid does not generate precipitation and stratification.
14. The processing system of claim 12,
the upper part of the pyrolysis furnace is of a cylindrical structure, the lower part of the pyrolysis furnace is of a conical structure, the cylindrical structure and the conical structure are isolated through an isolation unit, an organic combustible waste gas outlet is formed in the top of the cylindrical structure, and a pyrolysis ash outlet is formed in the bottom of the conical structure;
a stirring paddle is arranged in the cylindrical structure, and a stirring motor is arranged above the pyrolysis furnace to control the stirring paddle to rotate; the inside a plurality of steel balls that still are provided with of column structure, the stirring rake is right with 1 ~ 3 revolutions per minute's stirring speed under agitator motor's control the steel ball with get into the inside preparation liquid of column structure stirs, so that preparation liquid evenly distributed is in the surface of steel ball, it is right preparation liquid carries out the even heating, the steel ball can also be right the pyrolysis ash that produces grinds.
15. The treatment system according to claim 12, wherein the pyrolysis furnace is further provided with a nitrogen inlet through which nitrogen is filled during operation of the pyrolysis furnace so that the pyrolysis furnace and the ash discharge hopper are filled with nitrogen;
the pyrolysis furnace is also provided with a pressure controller to control the pressure in the pyrolysis furnace, a pressure gauge is arranged in the pressure controller to measure the pressure value in the pyrolysis furnace, the pressure controller is electrically connected with the tail gas fan, and the output power of the tail gas fan is interlocked with the negative pressure value in the pyrolysis furnace to control the negative pressure value in the pyrolysis furnace to be stabilized between-1 kPa and-4 kPa.
16. The treatment system of claim 12, further comprising a leak check device for performing a cold leak check on the pyrolysis furnace when the tail gas blower is activated to bring the pyrolysis furnace to a negative pressure value of-6 kPa to-9 kPa.
17. The processing system of claim 12,
the waste gas filtering device is arranged at an organic combustible waste gas outlet of the pyrolysis furnace and is used for filtering the organic combustible waste gas generated by the pyrolysis furnace and then charging the filtered organic combustible waste gas into the combustion furnace, and the waste gas filtering device is a sintered ceramic or sintered metal filter;
and a nitrogen back-blowing device is arranged at the top of the waste gas filtering device and is used for regularly back-blowing the waste gas filtering device.
18. The processing system of claim 12, further comprising a pyrolytic ash metering device and a shielded glove box;
one end of the pyrolytic ash metering device is connected with the ash discharge hopper, and the other end of the pyrolytic ash metering device is connected with the shielding glove box, so that the weight of pyrolytic ash fed into the waste barrel from the ash discharge hopper every time is controlled through the pyrolytic ash metering device;
the waste barrel is detachably arranged at the bottom of the shielding glove box, so that the pyrolytic ash in the ash discharge hopper is loaded into the waste barrel through the shielding glove box.
19. The treatment system of claim 12, wherein an oxygen flow meter is further arranged outside the combustion furnace, so that the oxygen content in the combustion furnace is controlled to be 8-12% by the oxygen flow meter, and the organic combustible waste gas can be completely combusted.
20. The treatment system of claim 12, wherein the scrubber tower comprises a primary scrubber tower and a secondary scrubber tower connected in series;
one end of the first-stage washing tower is connected with the quencher through a pipeline, and the other end of the first-stage washing tower is connected with the second-stage washing tower through a pipeline; the first-stage washing tower is provided with a first-stage washing circulating pump, and the second-stage washing tower is provided with a second-stage washing circulating pump;
the primary washing circulating pump is used for driving deionized water to circulate so as to wash the flue gas filled into the primary washing tower by the quencher, and the temperature of the flue gas is reduced to be lower than a third preset temperature;
and the secondary washing circulating pump is used for driving deionized water to circulate so as to wash the flue gas filled into the secondary washing tower from the primary washing tower again, and the temperature of the flue gas is reduced to be lower than a second preset temperature.
21. The treatment system of claim 20, further comprising a tail gas condenser, wherein one end of the tail gas condenser is connected to the secondary scrubber via a pipeline, and the other end of the tail gas condenser is connected to the tail gas fan via a pipeline; the tail gas condenser is used for further cooling the flue gas washed by the secondary washing tower by adopting chilled water so as to reduce the content of saturated wet steam in the flue gas;
the treatment system further comprises a flue gas filter, wherein the flue gas filter is arranged between the tail gas fan and the condenser and used for filtering flue gas cooled by the tail gas condenser, and the filtered flue gas is discharged by the tail gas fan.
22. The treatment system of claim 12, further comprising a waste reservoir and an additive dispensing tank;
the additive preparation tank is also provided with a cooling device, and the cooling device is used for controlling the temperature of the additive preparation tank to be not more than 100 ℃ in the additive preparation process;
the waste liquid storage tank is used for temporarily storing the radioactive organic waste liquid;
the additive preparation tank is communicated with the suspension liquid preparation tank through an additive pump and a pipeline; the waste liquid storage tank is communicated with the suspension liquid preparation tank through a waste liquid pump and a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010001755.9A CN111161900B (en) | 2020-01-02 | 2020-01-02 | Radioactive organic waste liquid treatment process and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010001755.9A CN111161900B (en) | 2020-01-02 | 2020-01-02 | Radioactive organic waste liquid treatment process and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111161900A true CN111161900A (en) | 2020-05-15 |
| CN111161900B CN111161900B (en) | 2022-04-29 |
Family
ID=70561147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010001755.9A Active CN111161900B (en) | 2020-01-02 | 2020-01-02 | Radioactive organic waste liquid treatment process and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111161900B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111681796A (en) * | 2020-06-12 | 2020-09-18 | 中国核电工程有限公司 | Radioactive waste material pyrolysis device |
| CN117259318A (en) * | 2023-11-17 | 2023-12-22 | 中国核电工程有限公司 | Dirty solvent treatment method, cleaning circulation method, treatment device and system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3234017A1 (en) * | 1982-09-14 | 1984-03-15 | Nukem Gmbh, 6450 Hanau | Continuous furnace for the incineration of solid organic substances |
| JP2013189609A (en) * | 2012-03-15 | 2013-09-26 | Osutorando:Kk | Pyrolytic gasifying method and pyrolytic gasifying apparatus of organic waste |
| CN103836633A (en) * | 2012-11-21 | 2014-06-04 | 中核建中核燃料元件有限公司 | Pyrolysis device applied to wasted TBP pyrolysis and incineration process |
| CN109830324A (en) * | 2019-01-17 | 2019-05-31 | 中国辐射防护研究院 | A kind of charging feed liquid and preparation method suitable for pyrolytic incineration method processing Radioactive myocardial damage |
| CN109824355A (en) * | 2019-02-22 | 2019-05-31 | 西南科技大学 | A kind of processing method of Spent Radioactive organic solvent tributyl phosphate pyrolysis ashes |
-
2020
- 2020-01-02 CN CN202010001755.9A patent/CN111161900B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3234017A1 (en) * | 1982-09-14 | 1984-03-15 | Nukem Gmbh, 6450 Hanau | Continuous furnace for the incineration of solid organic substances |
| JP2013189609A (en) * | 2012-03-15 | 2013-09-26 | Osutorando:Kk | Pyrolytic gasifying method and pyrolytic gasifying apparatus of organic waste |
| CN103836633A (en) * | 2012-11-21 | 2014-06-04 | 中核建中核燃料元件有限公司 | Pyrolysis device applied to wasted TBP pyrolysis and incineration process |
| CN109830324A (en) * | 2019-01-17 | 2019-05-31 | 中国辐射防护研究院 | A kind of charging feed liquid and preparation method suitable for pyrolytic incineration method processing Radioactive myocardial damage |
| CN109824355A (en) * | 2019-02-22 | 2019-05-31 | 西南科技大学 | A kind of processing method of Spent Radioactive organic solvent tributyl phosphate pyrolysis ashes |
Non-Patent Citations (3)
| Title |
|---|
| PAUL LUYCX ET AL.: "Pebble bed pyrolysis for the processing of alpha contaminated organic effluents", 《HTTP://ARCHIVE.WMSYM.ORG/1999/37/37-3.PDF》 * |
| 杨丽莉: "放射性废TBP处理技术", 《辐射防护通讯》 * |
| 范显华 等: "TBP-煤油热解燃烧冷台架试验", 《范显华 等》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111681796A (en) * | 2020-06-12 | 2020-09-18 | 中国核电工程有限公司 | Radioactive waste material pyrolysis device |
| CN117259318A (en) * | 2023-11-17 | 2023-12-22 | 中国核电工程有限公司 | Dirty solvent treatment method, cleaning circulation method, treatment device and system |
| CN117259318B (en) * | 2023-11-17 | 2024-02-23 | 中国核电工程有限公司 | Dirty solvent treatment method, cleaning circulation method, treatment device and system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111161900B (en) | 2022-04-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111161900B (en) | Radioactive organic waste liquid treatment process and system | |
| CN103608099A (en) | System and method for hydrothermal reaction | |
| CN102272521A (en) | Chemical cleaning method and system with steam injection | |
| KR100864904B1 (en) | Apparatus for making oil and generating electricity with used hot gas | |
| CN113102446A (en) | Pyrolysis furnace and pyrolysis system for treating waste incineration fly ash dioxin | |
| CN107384449A (en) | A kind of pyrolysis system and method for pyrolysis for three kinds of state materials of gas, liquid, solid | |
| WO2008030137A1 (en) | Method and device for processing rubber waste | |
| KR102158170B1 (en) | Semi-coke production system of bituminous coal | |
| CN207126967U (en) | Flying dust processing unit | |
| CN107143862A (en) | Circulating fluid bed garbage furnace low temperature superheater ash conveying device and method | |
| RU2560095C2 (en) | Method of recycling wastes containing uranium compounds | |
| CN209343792U (en) | Handle the process system of radioactivity debirs | |
| CN111667937A (en) | Steam reforming fixed bed reactor for treating radioactive waste | |
| CZ2013677A3 (en) | Process for producing fuels for power engineering and fuel producing apparatus | |
| CN110486958A (en) | Slot type photo-thermal power station fused salt injection technology | |
| CN104501173A (en) | Device and process for pyrolysis treatment on chemical-industry type solid waste and waste liquid | |
| JP2011174873A (en) | Treating device and method of radioactive waste | |
| CN104851469B (en) | Spirally whole bucket feeds processing system to one kind | |
| CN107848853B (en) | The method and apparatus of the semicontinuous pyrohydrolysis of sludge | |
| CN206875442U (en) | Circulating fluid bed garbage furnace low temperature superheater ash conveying device | |
| KR20170038490A (en) | Drying apparatus for recirculating the sludge heat, dart | |
| CN115148388A (en) | System for treating a radioactive organic phase-containing suspension | |
| CN110718315A (en) | Waste resin environment-friendly pyrolysis treatment device and treatment method thereof | |
| CN110257107A (en) | A kind of biomass pyrogenation gasification system coupling pulverized-coal fired boiler power station electricity-generating method | |
| CN106328237B (en) | A kind of carbonization of radioactive waste ion exchange resin microwave, cineration technics and dedicated unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |