EP0603708A2 - Procédé de combustion, séparation et solidification de 3H en 14C à partir de liquides combustibles - Google Patents

Procédé de combustion, séparation et solidification de 3H en 14C à partir de liquides combustibles Download PDF

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Publication number
EP0603708A2
EP0603708A2 EP93120118A EP93120118A EP0603708A2 EP 0603708 A2 EP0603708 A2 EP 0603708A2 EP 93120118 A EP93120118 A EP 93120118A EP 93120118 A EP93120118 A EP 93120118A EP 0603708 A2 EP0603708 A2 EP 0603708A2
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Prior art keywords
gaseous
stream
desiccating
liquid
produce
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EP93120118A
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German (de)
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EP0603708A3 (fr
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Steven T. Schaeffer
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EIDP Inc
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EI Du Pont de Nemours and Co
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    • 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
    • G21F9/30—Processing
    • G21F9/32—Processing by incineration
    • 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

Definitions

  • This invention relates to a process for removing tritium (3H) and carbon-14 (14C) from combustible liquids, and more particularly to a process for the combustion, separation, and solidification of 3H and 14C from combustible liquids.
  • radiochemicals for use in various applications such as medical tracer compounds and diagnostic reagents
  • processes including precursor synthesis, radiolabelling, and final purification.
  • these processes result in the production of radioactive by-products and radioactive contaminated solvents which are eventually separated from the final product.
  • radioactive wastes are isolated and, depending on their nature, either disposed of or stored at the site of generation.
  • Radioactive wastes from the processing of 32P, 33P, and 35S can be stored at the site of generation for eventual decay due to their relatively short half-lives.
  • the longer half-lives of 3H and 14C make on-site storage of these radioactive wastes costly and also pose a safety hazard.
  • Radioactive liquid streams containing 3H and/or 14C can be disposed of in a variety ways.
  • aqueous wastes containing 0.5% organics may be mixed with cement and subsequently buried.
  • Organic wastes containing less than 0.2 milli Curie (mCi) radioactivity due to the presence of 3H and/or 14C can usually be burned, and some facilities may provide for combustion of wastes having radioactive contamination as high as 0.2 to 1.0 mCi/gallon.
  • Japanese Patent Application 59035197 published February 25, 1984 discloses a controlled process for incinerating organic liquid streams contaminated by radioactive 3H and 14C which utilizes a liquid valve for regulating the organic solvent waste liquid and/or ignition oil flowing into the burners of the incinerator, so that the ignition oil is fed before or after the end of the incineration of the waste liquid.
  • Japanese Patent Application J02287299 published November 27, 1990, discloses a method for treating radioactive wastes containing 14C in which hydrogen peroxide is reacted with the radioactive waste in an aqueous medium in the presence of a water soluble oxygen containing organic compound and copper and/or iron ions to produce a gaseous 14CO2 stream which is contacted with barium hydroxide to produce barium carbonate.
  • the remaining 14CO2 gas-free solution can be solidified with cement or asphalt.
  • Japanese Patent Application JP04093797 discloses a process for treating gaseous 14CO2 generated by nuclear power plants by passing the 14CO2 through an organic solvent or by spraying the organic solvent into the 14CO2, mixing the organic solvent with a monomer, and forming a plastic product via polymerization.
  • U.S. Patent No. 4,555,361 issued November 26, 1985 to Buckely et al. discloses a method for reducing the volume of solid radioactive waste by pyrolysis of the radioactive waste, followed by gasification of residual carbon with superheated steam, so that carbon containing components of the waste are removed as gaseous decomposition products in the form of carbon containing components in the form of carbon monoxide and hydrogen, leaving an ash residue for subsequent disposal.
  • Publication EP 265744 published May 4, 1988, discloses a method for removing 3H from gas mixtures by hydrogenation of the 3H with a mono or poly-unsaturated compound such as linoleic acid in a Pt or Pd catalyst.
  • Japanese Patent Application J53126497 published April 11, 1978, discloses a process for removing gaseous 3H by absorption of the 3H in an absorption tower filled with an intermetallic compound composed of a rare earth metal and Ni, such as LaNi5.
  • Liquid wastes containing greater than 0.5% organics and further having greater than 1.0 mCi/gallon radioactivity present novel disposal difficulties. These wastes, hereinafter referred to as “mixed wastes", contain hazardous (organic) components as well as radioactive contamination. New technologies for treating such mixed wastes are under development. Generally, mixed wastes cannot be accepted for burial due to their relatively high organic content and cannot be combusted safely due to their high radioactivity. For example, Dhoogie, P.M. A Catalytic Wet Oxidation Process For Mixed Waste Volume Reduction/Recycling, "Proceedings of the Symposium on Waste Management," Arlington, AZ, March 1, 1992, R. G. Post, Editor p.
  • This invention relates to process for the removal of 3H and 14C from a combustible liquid stream which comprises:
  • the invention relates to a process wherein after step(b) above, any remaining gaseous 3H2O is removed by contacting the gaseous stream with a desiccating agent.
  • Another aspect of the invention relates to a process for the removal of 3H and 14C from a combustible liquid stream which comprises:
  • Yet another aspect of the invention relates to a process for the removal of 3H and 14C from a combustible liquid stream which comprises:
  • the invention relates to the above process wherein after step (b) remaining gaseous 3H2O is removed by passing the gaseous 3H2O through a desiccating column, the desiccating column having a desiccating agent contained therein.
  • a final aspect of the invention relates to a process for the removal of 3H and 14C from a combustible liquid stream which comprises:
  • Figure 1 depicts a flow chart for a process to remove 3H and 14C present in a combustible liquid stream.
  • the process depicted includes combustion of the radioactive stream to produce 14CO2 and 3H2O, removal of the 3H2O by condensation followed by removal of any remaining 3H2O through the use of a desiccating agent, absorption of the 14CO2 by a caustic solution to produce a 14C salt, and solidification of the 14C salt and 3H2O liquid.
  • This invention relates to a process for the removal of 3H and 14C from a combustible liquid stream which comprises combusting a combustible liquid containing 3H and 14C to produce a gaseous stream containing 3H2O and 14CO2, condensing the gaseous 3H2O to produce a liquid 3H2O stream, absorbing the gaseous 14CO2 with a caustic solution to produce a 14C salt, and solidifying the liquid 3H2O stream and the 14C salt through the addition of a solidifying agent.
  • the gaseous 3H2O can be removed from the gaseous stream containing the 3H2O and 14CO2 by contacting the gaseous stream with a desiccating agent.
  • a furnace system can be used for the combustion process.
  • Such a furnace system includes one or more burners which are the devices used for producing a flame.
  • the burner mixes the combustible liquid stream to be combusted and an oxidizer in proportions that are within the limits of flammability for ignition as well as for steady combustion.
  • the furnace can be defined as the enclosed space in which the chemical oxidation of the combustible liquid is achieved.
  • the furnace complements the burner or burners firing into it to obtain the desired combustion reaction.
  • the furnace and burner combination should be designed so as to provide for the four elements of good combustion, including intimate mixing of the combustible liquid stream to be combusted and the oxidizer, admission of sufficient oxidizer to burn the combutible liquid stream completely, sufficient temperature to ignite the combustible liquid stream/air mixture and complete its combustion, and the required residence time for combustion to be complete (see Perry, R. H., and and Chilton, C. H., Chemical Engineers' Handbook, New York (1973)).
  • combustion liquid stream is meant any liquid stream which is combustible or which can be rendered combustible.
  • combustionible is meant the ability to be burned (oxidized) to produce the products of combustion, including water (H2O) and carbon dioxide (CO2) gases, and any solid ash wastes remaining after completion of the oxidation process.
  • Preferred liquids to be combusted are mixed wastes.
  • mixed waste is meant liquid wastes containing hazardous (organic) components as well as radioactive contamination.
  • the preferred liquid mixed wastes treated by the method of the present invention are those mixed wastes containing greater than 0.5% organics and further having greater than 1.0 mCi/gallon radioactivity.
  • An example of a composition of such a preferred mixed waste to be combusted is shown in Table 1, Flow 1 and depicted in Figure 1, Flow 1.
  • Drums containing the liquid stream to be combusted are preferably first transferred to a liquid waste feed tank using a liquid transport means such as a drum pump. Upon being opened, these drums can be vacuumed into the furnace air feed system to combust any volatiles.
  • the liquid to be combusted can be pumped as a feed stream into the furnace at various rates depending on known operating parameters including liquid feed stream rate, furnace capacity, and furnace operating pressure and temperature.
  • the liquid to be combusted can be withdrawn from the bottom of the drum and from just below the liquid level to form the feed stream to insure that no dramatic transitions in British Thermal Units (BTU) value occur upon feeding of the liquid stream to be combusted to the furnace.
  • BTU British Thermal Units
  • An organic fuel can be added to the liquid stream to be combusted in order to increase the BTU value of the liquid stream to be combusted.
  • Any fuel can be used which, when added to the liquid stream to be combusted has the effect of rendering the liquid stream to be combusted a combustible liquid stream, thereby insuring uniform combustion (oxidation).
  • Such added fuels serve to boost the BTU value of the liquid stream to be combusted.
  • the heat of combustion of the combustible liquid should be about 90,000 BTU/gal or greater.
  • suitable fuels include propane, ethane, butane, natural gas and fuel oil.
  • propane is used as the fuel.
  • the desired heat of combustion (approximately 90,000 BTU/gallon) can be used to determine a suitable propane feed rate to the furnace. While this flow rate can be varied to control the furnace operating temperature, the propane addition rate should be minimized to avoid excessive non-radioactive H2O and CO2 generation which can lead to increased waste to disposal volume ratio. Similarly, the desired flow rate for other fuels can be determined based on their specific heats of combustion and a liquid combustible stream having a desired heat of combustion of about of 90,000 BTU/gal.
  • Air can be supplied via an air compressor to the furnace at various rates depending on the scale of design. An air ratio corresponding to 50% excess air over the theoretical amount of air required to burn (combust) the carbon and net hydrogen in the liquid combustible stream is preferred.
  • the air compressor inlet can be dampered to the open air, thereby providing for a means of suction via flexible hose to any storage drums and tanks which could release radioactive volatiles.
  • the gaseous stream exiting the furnace contains the products of combustion, including carbon dioxide, water, nitrogen, and oxygen.
  • Any 14C originally in the combustible liquid is in the form of radioactive carbon dioxide (14CO2) and any 3H originally present in the combustible liquid is in the form of radioactive water (3H2O).
  • the flow rate of the gaseous stream exiting the furnace hereinafter referred to as the "gaseous stream containing 3H2O and 14CO2" can vary widely depending upon scale of design and desired operating conditions.
  • the furnace can be operated under pressure, preferably, at about 10 pounds per square inch gauge (psig).
  • a furnace heat exchanger can be used to cool the gaseous stream containing the 14CO2 and 3H2O combustion gases prior to the removal of the 3H2O and the adsorption of the 14CO2.
  • the furnace heat exchanger cools the gaseous stream containing the 14CO2 and 3H2O to 400° F and generates 15.6 pounds/minute (lb/min) saturated steam at 150 psig.
  • the gaseous stream containing the 14CO2 and 3H2O is passed through a condenser to cool the gas mixture and condense a portion of the water vapor.
  • a condenser capable of providing sufficient cooling to condense a substantial portion the water present in the gaseous stream containing the 14CO2 and 3H2O can be used.
  • the heat exchanger can be sized using known heat transfer principles and heat exchanger design parameters to provide, preferably, for cooling the gas mixture to 68°F and condensing 83% of the gaseous H2O (including 3H2O) to produce a liquid 3H2O stream. This stream will also contain nonradioactive H2O.
  • Cooling can, for example, be provided by counter-current flow of water at 59°F, either from an existing cooling tower or from an independent refrigeration system.
  • a suitable types of heat exchangers for use with this process include spiral heat exchangers and shell-and-tube exchangers.
  • liquid 3H2O stream The condensate from the exchanger containing the liquid 3H2O, referred to as the "liquid 3H2O stream", can be collected for later incorporation into the final solidification step (see below).
  • a desiccating column or columns containing a desiccating agent can be used to remove any of the gaseous 3H2O remaining after condensation.
  • the desiccating column(s) can be omitted from the process of the present invention.
  • the condenser can be omitted and the use of a desiccating column or columns can utilized as the sole means for removal of gaseous 3H2O.
  • Sodium sulfate (Na2SO4) is the preferred desiccating agent.
  • a moisture sensor at the column outlet can be used to indicate an increase in the exit gaseous water content which is used as a signal to take a water saturated desiccating column off-line and have it regenerated. If the condenser is operated at 68°F the desiccating column should be regenerated approximately every 3 days; more frequently if the condenser is operated at greater than 68°F.
  • Regeneration of the desiccant can be performed by purging the column either with the furnace exist gas (gaseous stream containing the 14CO2 and 3H2O) or by passing heated air, preferably at about 300°F, through the column.
  • the hot gas releases the water from the desiccating agent, and the released water can be recycled to the condenser inlet.
  • a moisture sensor at the column outlet can be used to indicate completion of the regeneration process.
  • two vertical desiccating columns are utilized to allow for the desiccation operation to continue while a water saturated column is being regenerated.
  • regeneration is performed in a first desiccating column by purging the column with the furnace exit gas and sending the released water to the condenser inlet, while a second desiccating column downstream of the condenser is utilized to absorb any remaining gaseous H2O.
  • the gaseous CO2 present in the stream exiting the desiccating column is then sent through a scrubber or scrubbers, wherein the CO2 is absorbed (at least some of the CO2 is 14CO2).
  • absorption is meant the removal of CO2 (including 14CO2) from the gaseous stream by reaction of the CO2 with a liquid solution to produce a non-reactive non-volatile product.
  • Methods for sizing and optimizing caustic scrubbers for removal of CO2 are known. Such methods are described by Perry, R. H., and Chilton, C. H., Chemical Engineers' Handbook, section 20, New York (1973), the disclosure of which is hereby incorporated by reference.
  • scrubber any type of equipment designed for gas-liquid contacting including various types of plate columns, packed columns, falling film (wetted wall columns), fluidized bed columns, spray chambers, agitated vessels, and line mixers.
  • a vertical scrubber or scrubbers is used, the vertical scrubber having a packed column packed with suitable size packing, such as, for example, one inch Raschig rings.
  • suitable size packing such as, for example, one inch Raschig rings.
  • Raschig rings Raschig rings, pall rings, berl saddles, lessing rings, intalox saddles, and tellerettes.
  • the type of packing used can be chosen using known packing properties such as those relating to surface availability, interface regeneration, pressure drop, weight, and corrosion resistance.
  • the packed column can be designed as a cylindrical shell containing a support plate for the packing material and a liquid distributing device designed to provide effective irrigation of the packing. Devices can be added to the packed column for redistribution of any liquid that might channel down the sides of the column. Preferably two vertical packed column scrubbers are used in sequence.
  • These scrubber(s) contact the gaseous 14CO2 with a caustic solution, preferably NaOH, and preferably in a countercurrent flow with the stream containing gaseous 14CO2 so that the 14CO2 is reacted with the caustic solution to form a 14C salt such as sodium carbonate (Na214CO3) (when the caustic solution utilized is NaOH).
  • a 14C salt such as sodium carbonate (Na214CO3) (when the caustic solution utilized is NaOH).
  • Non-radioactive CO2 will similarly react with the caustic solution to form a non-radioactive salt (Na2CO3).
  • the scrubber(s) can be sized using known mass transfer principles and taking into account various factors such as pressure drop and mass transfer of the gaseous 14CO2 accompanied by chemical reaction with the caustic solution. When two scrubbers are used sequentially each scrubber can be designed, preferably, to remove 96% of the CO2 for a total removal rate of 99.84% of the inlet 14CO2.
  • the 14C salt exiting the scrubber(s) is in the form of a slurry solution which can be fed, preferably, into a common holding tank.
  • the slurry can be pumped through any properly sized heat exchanger to remove any heat of reaction generated by reaction with the caustic solution.
  • the slurry can then be filtered.
  • Various filtration processes can be utilized including centrifugal filtration, plate and frame filtration, pressure and vacuum leaf filtration, and rotary drum filtration.
  • Known principles of filtration and factors for sizing filters are described by Perry, R. H., and Chilton, C. H., Chemical Engineers' Handbook, section 19, New York (1973), the disclosure of which is hereby incorporated by reference.
  • the filter used is a rotary disk filter.
  • the 14C salt for example, sodium carbonate
  • the rotary disk filter can be designed and the operating parameters chosen, using known methods, such that the filter cake can preferably consist of about 30% solids.
  • the filter cake can be continuously removed from the rotary disk filter and directed to a mixer.
  • the liquid 3H2O and/or the 30% solid 14C salt containing slurry are then combined with a solidifying agent.
  • the solidifying agent is any substance which solidifies or hardens the liquid 3H2O and/or the 30% solid 14C salt containing slurry for disposal.
  • the solidifying agent should be chosen so as to insure that no leaching of radiactivity can occur for extended period of time, preferably 500 years or more.
  • a variety of solidifying agents can be used including cement, glass, urea-formaldehyde, polybutadiene, polyester-epoxy, acrylamide gel, polyolefin, and polyurethane.
  • the solidifying agent utilized is cement.
  • Portland cement is basically a calcium silicate mixture containing predominantly tricalcium and dicalcium silicates with small amounts of tricalcium aluminate and a calcium aluminoferrite.
  • the process of the present invention can be modified for exclusive processing of either 14C or 3H contaminants.
  • a condenser can be used to cool the gas to 86°F and the desiccating column(s) can be by-passed.
  • the waste disposal volume increase will only be slightly affected unless cement recipes othe than the described Portland cement recipe (see Figure 1, Flows 26 and 27) are used.
  • the scrubber(s) can be by-passed and the gas exiting the desiccation column can be fed directly into dilution ducts for subsequent dispersion.
  • the waste disposal volume increase will be reduced considerably by this type of processing.
  • the present invention thus provides a process for treating liquids containing both organic wastes as well as radioactive contamination due the presence of 14C or 3H contaminants, in a way that allows for the safe disposal of such liquids in a single process.
  • Figure 1 depicts a process flow chart for the preferred embodiment of the present invention.
  • the flow streams, and processing equipment are described in the example below.
  • the gas flow exiting a furnace 30, (gaseous stream containing 3H2O and 14CO 2) (Fig 1, Flow 4) is 300 cubic feet per minute (cu. ft./min) at standard operating temperature and pressure (STP).
  • Propane is added at compressor 32 as the auxiliary fuel (Fig 1, Flow 2) to boost the BTU value of the mixed waste.
  • the furnace operates at 10 pounds per square inch gauge (psig).
  • the particular liquid to be combusted is a mixed waste of the composition shown in Table 1 and depicted in Figure 1, Flow 1.
  • Drums containing liquid mixed waste (Figure 1, Flow 1) are first transferred to a mixed waste feed tank at 34 using a drum pump at 36. The opening of these drums is vacuumed into the furnace air-feed system to combust any volatiles which may be present.
  • the mixed waste feed tank, 34 maintained under a partial vacuum via the furnace air-feed system ( Figure 1, Flow 3), with air being added at compressor 38, the mixed waste is pumped into the furnace, 30, at a rate of 0.178 gal/min.
  • the liquid to be combusted is withdrawn from the bottom of the drum and from just below the liquid level to insure that no dramatic transitions will occur in BTU value.
  • propane is utilized to increase the BTU value of the contaminated liquid stream.
  • the approximate molar ratio of propane to mixed waste is 9:100, thereby yielding a 90,000 BTU/gal liquid fuel.
  • This ratio corresponds to a propane flow rate which is 1.5 cu. ft/min (STP). While this flow rate can be varied to control the furnace operating temperature, the propane addition rate should be minimized to avoid excessive non-radioactive H2O and CO2 generation which can lead to increased contaminated waste-to-disposal volume ratio.
  • Air is supplied to the furnace at a rate of 281 cu. ft/min (STP) corresponding to 50% excess air for the reaction. This air ratio insures complete combustion of the mixed waste.
  • STP ft/min
  • the air compressor inlet is dampered to the open air and permits suction via flexible hose to any storage drums and tanks which could release radioactive volatiles.
  • the furnace heat exchanger, 40 (Figure 1, HX 1) cools the gaseous stream containing the 3H2O and 14CO2 to 400°F and generates 15.6 lb/min of saturated steam at 150 psig (366°F) ( Figure 1 Flow 6). The net heat transferred is 13,600 BTU/min.
  • the gaseous stream containing the 3H2O and 14CO2 then passes through a first desiccating column, 42, (Fig. 1, DES COL. 1) which is shown in Fig. 1 operating in a regeneration mode.
  • Regeneration of the desiccating agent is completed by purging with the furnace exit gas ( Figure 1, Flow 7).
  • Hot air can also be used to purge the desiccating column 42.
  • the hot furnace exit gas releases the water from the desiccating agent for recycle to the condenser inlet.
  • a moisture sensor at the outlet of the desiccating column 42 indicates completion of the regeneration process.
  • the gaseous stream exiting the desiccating column 42 then passes through a spiral heat exchanger, 44, (80 square feet) (Figure 1, COND, Flow 8) to cool the gas mixture to 68°F and condense 83% of the water vapor.
  • the net heat transfer in the exchanger is 3600 BTU/min. Cooling is provided by counter-current flow of water at the cooler, 48 ( Figure 1, COOLER, Flow 11).
  • the condensate containing liquid 3H2O from the condenser 44 is collected for later solidification into a cement matrix ( Figure 1, Flow 9).
  • the gaseous stream exiting the condenser 44 then enters a second 3.3' dia x 15' vertical desiccating column, 46, ( Figure 1, DES COL 2, Flow 10) packed with 12,100 lbs of calcium sulfate (CaSO4).
  • a moisture sensor at the column outlet indicates an increase in the water content (approximately every 3 days, more frequently if the condenser is operated at greater than 68°F)
  • the column 46 is taken off-line and regenerated.
  • the gaseous stream exiting the second desiccating column, 46, gas then enters a series of two vertical packed column scrubbers at 50 and 52 (Figure 1, SCRUB COL 1 and SCRUB COL 2, Flows 13 and 15), which are 1.9 feet (') in diameter x 22' in length and packed with 1" Raschig rings.
  • These scrubbers at 50 and 52 contact the entering gaseous stream with 177 pounds per minute (lb/min) NaOH solution ( Figure 1, Flows 23, 14, and 17) to provide for the reaction of the CO2 to produce the 14C salt, sodium carbonate.
  • Each scrubber at 50 and 52 sequentially removes 96% of the CO2 for a total removal rate of 99.84% of the inlet CO2 corresponding to an annual release rate of 14CO2 of 3.4 Ci/yr. Exiting the scrubber 52 is 247 cu. ft./min (STP) CO2-free gas ( Figure 1, Flow 18) for dilution in facility main ducts.
  • the filtrate in the holding tank 62 is adjusted to 2 Normal (N) NaOH by addition of 11 lb/min of 50 weight% NaOH ( Figure 1, Flow 22).
  • the tank level is maintained by addition of water to the holding tank 62.
  • the caustic solution is returned to the tops of the scrubbers 50 and 52, by two feed pumps at 64 operating at 177 lb/min ( Figure 1, Flow 23 (combined), 14, and 17).
  • the rate of drum generation, and therefore the waste-to-disposal volume ratio can be reduced significantly if the filter can further concentrate the solids.
  • the final drum mixture for the process described averages 5.1 gallons of mixed waste (volume increase of 9.8 fold), and 2.2 Ci 3H and 0.17 Ci 14C.
  • Table 1 provides a material and energy balance of the exemplified process. Flow numbers referred to above correspond to the labelled streams of Figure 1.

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  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • High Energy & Nuclear Physics (AREA)
  • Environmental & Geological Engineering (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
EP19930120118 1992-12-18 1993-12-14 Procédé de combustion, séparation et solidification de 3H en 14C à partir de liquides combustibles Withdrawn EP0603708A3 (fr)

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WO2003008960A2 (fr) * 2001-07-17 2003-01-30 British Nuclear Fuels Plc Technique analytique
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CN113270215A (zh) * 2021-05-18 2021-08-17 清华大学 核电厂液态流出物14c自动前处理装置及处理方法

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FR2943167B1 (fr) * 2009-03-11 2011-03-25 Electricite De France Traitement de dechets radioactifs carbones.
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CN110941005B (zh) * 2019-12-06 2021-07-20 苏州热工研究院有限公司 一种空气中碳-14在线连续监测装置及空气中碳-14活度浓度的计算方法

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WO2003008960A2 (fr) * 2001-07-17 2003-01-30 British Nuclear Fuels Plc Technique analytique
WO2003008960A3 (fr) * 2001-07-17 2003-12-31 British Nuclear Fuels Plc Technique analytique
CN109727689A (zh) * 2019-01-16 2019-05-07 哈尔滨理工大学 一种模拟氦气风机驱动电机工作环境的环路系统
CN113270215A (zh) * 2021-05-18 2021-08-17 清华大学 核电厂液态流出物14c自动前处理装置及处理方法
CN113270215B (zh) * 2021-05-18 2022-12-09 清华大学 核电厂液态流出物14c自动前处理装置及处理方法

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EP0603708A3 (fr) 1994-07-27

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