WO2016198654A1 - Installation, procédé de dénitration thermique, utilisation d'une telle installation et produit obtenu par un tel procédé - Google Patents
Installation, procédé de dénitration thermique, utilisation d'une telle installation et produit obtenu par un tel procédé Download PDFInfo
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- WO2016198654A1 WO2016198654A1 PCT/EP2016/063377 EP2016063377W WO2016198654A1 WO 2016198654 A1 WO2016198654 A1 WO 2016198654A1 EP 2016063377 W EP2016063377 W EP 2016063377W WO 2016198654 A1 WO2016198654 A1 WO 2016198654A1
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- reaction chamber
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- 238000000034 method Methods 0.000 title claims abstract description 30
- 230000008569 process Effects 0.000 title claims abstract description 18
- JCMLRUNDSXARRW-UHFFFAOYSA-N trioxouranium Chemical compound O=[U](=O)=O JCMLRUNDSXARRW-UHFFFAOYSA-N 0.000 claims abstract description 180
- 239000002245 particle Substances 0.000 claims abstract description 124
- 239000007789 gas Substances 0.000 claims abstract description 102
- 238000006243 chemical reaction Methods 0.000 claims abstract description 100
- 238000000926 separation method Methods 0.000 claims abstract description 93
- 229910002007 uranyl nitrate Inorganic materials 0.000 claims abstract description 34
- FGHSTPNOXKDLKU-UHFFFAOYSA-N nitric acid;hydrate Chemical compound O.O[N+]([O-])=O FGHSTPNOXKDLKU-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000009434 installation Methods 0.000 claims description 71
- FCTBKIHDJGHPPO-UHFFFAOYSA-N uranium dioxide Inorganic materials O=[U]=O FCTBKIHDJGHPPO-UHFFFAOYSA-N 0.000 claims description 19
- 229910002651 NO3 Inorganic materials 0.000 claims description 15
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 14
- 229940077390 uranyl nitrate hexahydrate Drugs 0.000 claims description 11
- VEMKTZHHVJILDY-PMACEKPBSA-N (5-benzylfuran-3-yl)methyl (1r,3s)-2,2-dimethyl-3-(2-methylprop-1-enyl)cyclopropane-1-carboxylate Chemical group CC1(C)[C@@H](C=C(C)C)[C@H]1C(=O)OCC1=COC(CC=2C=CC=CC=2)=C1 VEMKTZHHVJILDY-PMACEKPBSA-N 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 8
- 238000010908 decantation Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 4
- 150000002500 ions Chemical class 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 230000036961 partial effect Effects 0.000 claims description 3
- 125000005289 uranyl group Chemical group 0.000 claims description 3
- 229910009112 xH2O Inorganic materials 0.000 claims 1
- 238000003786 synthesis reaction Methods 0.000 description 12
- 230000015572 biosynthetic process Effects 0.000 description 11
- 239000000203 mixture Substances 0.000 description 7
- OOAWCECZEHPMBX-UHFFFAOYSA-N oxygen(2-);uranium(4+) Chemical compound [O-2].[O-2].[U+4] OOAWCECZEHPMBX-UHFFFAOYSA-N 0.000 description 7
- 230000009257 reactivity Effects 0.000 description 7
- 230000005484 gravity Effects 0.000 description 6
- 230000000877 morphologic effect Effects 0.000 description 6
- 230000000295 complement effect Effects 0.000 description 5
- MZFRHHGRNOIMLW-UHFFFAOYSA-J uranium(4+);tetrafluoride Chemical compound F[U](F)(F)F MZFRHHGRNOIMLW-UHFFFAOYSA-J 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 230000000875 corresponding effect Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- -1 nitrate hydrate uranium trioxide Chemical compound 0.000 description 4
- 239000012159 carrier gas Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 230000000670 limiting effect Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000011824 nuclear material Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000002829 reductive effect Effects 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 238000004438 BET method Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 230000005284 excitation Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000003682 fluorination reaction Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000004043 responsiveness Effects 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 230000000930 thermomechanical effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D39/00—Filtering material for liquid or gaseous fluids
- B01D39/14—Other self-supporting filtering material ; Other filtering material
- B01D39/20—Other self-supporting filtering material ; Other filtering material of inorganic material, e.g. asbestos paper, metallic filtering material of non-woven wires
- B01D39/2027—Metallic material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
- B01D45/08—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D49/00—Separating dispersed particles from gases, air or vapours by other methods
- B01D49/003—Separating dispersed particles from gases, air or vapours by other methods by sedimentation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/002—Nozzle-type elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/008—Pyrolysis reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/006—Separating solid material from the gas/liquid stream by filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/007—Separating solid material from the gas/liquid stream by sedimentation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G43/00—Compounds of uranium
- C01G43/01—Oxides; Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00157—Controlling the temperature by means of a burner
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
- B01J2219/194—Details relating to the geometry of the reactor round
- B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
- B01J2219/1946—Details relating to the geometry of the reactor round circular or disk-shaped conical
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/12—Surface area
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
- C01P2006/82—Compositional purity water content
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E30/00—Energy generation of nuclear origin
- Y02E30/30—Nuclear fission reactors
Definitions
- the present invention relates to a thermal denitration plant of uranyl nitrate hydrate to obtain uranium trioxide, the uranium dioxide being in the form of particles.
- the invention also relates to a use of such an installation for carrying out a thermal denitration of a hydrated uranyl nitrate, in particular the thermal denitration of uranyl nitrate hexahydrate.
- the present invention also relates to a method of thermal denitration of uranyl nitrate hydrate to uranium trioxide, as well as to uranium trioxide obtained directly by this thermal denitration process, this uranium dioxide occurring in the form of particles.
- the uranium trioxide UO3 obtained can then be reduced to uranium dioxide U0 2 .
- this uranium dioxide UO2 can then be converted into uranium tetrafluoride UF 4 which plays a major role in various processes of the nuclear industry.
- the document [2] describes, moreover, a thermal denitration plant uranyl nitrate suitable for carrying out the above process.
- This plant shown schematically in Figure 1 attached and described in connection with the thermal denitration of uranyl nitrate hexahydrate, comprises:
- reaction chamber 1 disposed at the outlet of the burner 4 and comprising an uranyl nitrate hexahydrate inlet and configured to perform a thermal denitration of the uranyl nitrate hexahydrate and to form uranium trioxide UO3 in the form of particles ,
- a separation chamber 8 adapted to separate a part of the U03 particles from the gases resulting from the thermal denitration carried out in the reaction chamber 1, and
- the reaction chamber 1 is delimited by a cylindrical envelope extended at each end by a cone reducing the inlet 2 and outlet 3 sections of the reaction chamber 1.
- the inlet 2 is connected to a burner 4 fed with air through line 5 and with fuel gas via line 6.
- a line 7 supplies the reaction chamber 1 with uranyl nitrate hexahydrate.
- the outlet 3 of the reaction chamber 1 is connected, via a pipe 9, to the separation chamber 8 which is constituted by a cyclone.
- the particles of U03 formed in the reaction chamber 1 those having an average particle diameter of at least 15 ⁇ are recovered by the pipe 10 connected to the low output of the cyclone 8.
- the other particles, of average diameter lower particles, called fine particles, are conveyed by the gaseous vents at the top of the cyclone 8 and are sent through the pipe 11 to the filter 12 which is a bag filter.
- the fine particles are recovered by the pipe 13.
- the dust-free gases are sucked, by means of a fan situated at the outlet of the filter 12, via a pipe 14.
- U03 particles are collected by means of, not just a single pipe, but two pipes, in this case pipes 10 and 13.
- the UO3 particles obtained by this method have an average particle diameter not exceeding 5 ⁇ , the separation yield obtained by means of the cyclone 8 is low, typically of the order of 30%, the major part of the U03 particles being collected by the bag filter 12 and collected at the level of the pipe 13. Consequently, the implementation of an installation such as that described in the document [2] leads to a permanent overload of the bag filter 12. It should also be noted that the overload occurs, even in the case where the bag filter 12 is equipped with a continuous declogging device. Such an overload of the bag filter 12 generates a pressure drop which can be detrimental in the case of a facility for the treatment of nuclear material.
- the material constituting the sleeves of the bag filter 12 degrades from operating temperatures of the order of 200 ° C. Knowing that the denitration reaction temperature is between 350 ° C and 500 ° C, it is therefore imperative to cool the gas stream flowing in the pipe 11 by a complementary fresh air circulation device whose flow is typically of the order of 300 kg / h.
- the U03 particles collected at the pipe 10 connected to the cyclone 8 have a BET specific surface area of the order of 20 to 25 m 2 / g. These UO 3 particles thus have a very good reactivity with a view to their subsequent conversion to uranium dioxide U0 2 and uranium tetrafluoride UF 4 .
- the U03 particles collected at the pipe 13 connected to the bag filter 12 have, for their part, a BET specific surface area of less than 12 m 2 / g.
- the particles of U03 collected at the pipe 13 thus have a less efficient reactivity for their transformation in U0 2 then in UF 4 than those collected at the level of the pipe 13.
- the object of the invention is, therefore, to overcome the disadvantages of the prior art installation and to propose a thermal denitration plant uranyl nitrate hydrate uranium trioxide that allows to obtain with a high yield, uranium trioxide particles having morphological characteristics superior to the morphological characteristics exhibited by the mixture of the uranium trioxide particles collected at the line 10 disposed at the outlet of the separation chamber or cyclone 8, on the one hand, and those collected at the line 13 disposed at the outlet of the baghouse 12 of the installation described in document [2].
- the installation according to the invention must, in addition, have a configuration simplified compared to that of the installation described in document [2], avoiding in particular the implementation of complementary devices for cooling some of the gas flows.
- reaction chamber disposed at the outlet of the burner and comprising a hydrated uranyl nitrate inlet, said reaction chamber and the burner being configured to carry out a thermal denitration of the uranyl nitrate hydrate and to form uranium trioxide UO3; presenting in the form of particles,
- a separation chamber adapted to separate a part of the U03 particles from the gases resulting from the thermal denitration carried out in the reaction chamber
- At least one filter configured to separate the other part of the U03 particles from said gases and thus purify said gases.
- the separation chamber of the installation is a settling chamber into which the reaction chamber directly opens and the filter is able to perform the separation at a temperature above 350 ° C.
- settling chamber an enclosure having defined dimensions and a volume in which is introduced a mixture immiscible, such as solid particles contained in a carrier gas, and which uses the effect of gravity to separate the different phases, that is to say to separate the particles of the carrier gas.
- a mixture immiscible such as solid particles contained in a carrier gas
- gravity uses the effect of gravity to separate the different phases, that is to say to separate the particles of the carrier gas.
- a settling chamber as a separation chamber allows a particularly efficient separation of the U03 particles formed in the reaction chamber by thermal denitration of uranyl nitrate hydrate from the reaction gases. Indeed, the majority of the UO3 particles are collected at the outlet of the settling chamber, typically with a yield of at least 65%, a yield well above that of 30% obtained by the cyclone 8 of the installation described in document [2]. As a result, overloading of the filter or filters is avoided, which makes it possible to overcome all the disadvantages associated with the pressure drop generated by the overloading of the bag filter described in document [2].
- the inventors have also observed that, unexpectedly and surprisingly, the UO3 particles collected at the outlet of the settling chamber have morphological characteristics greater than those of the mixture of UO3 particles collected by means of the described installation. in document [2].
- these particles may have the following characteristics:
- the UO3 particles collected at the outlet of the settling chamber have a reactivity that is perfectly adapted for their subsequent conversion into uranium dioxide UO 2 and uranium tetrafluoride UF 4 .
- the upper part of the separation chamber may comprise at least one gas outlet equipped with the filter to evacuate the gases after their separation from the particles.
- the separation chamber may comprise at least one gas outlet in the direction of the filter.
- the plant may further include a gas deflection means for diverting gases from the mouth of the reaction chamber into the separation chamber at a settling location of the separation chamber having a lower vertical dimension. to that of the exit of gases.
- Such a deflection means makes it possible to optimize the separation efficiency of the separation chamber. Indeed, since the gases and particles are deflected by the deflection means on the deflection location having a vertical dimension lower than that of the filter, only the finest particles entrained by the hot gases are likely to reach the filter and not to be separated from the gases.
- separation chamber and "settling chamber” are used in turn to designate the separation chamber of the installation according to the invention and are therefore interchangeable, without changing the meaning.
- the vertical dimension of the settling place may be smaller than that of the gas outlet of a height h, the separation chamber having a height H.
- the ratio h on H may be between 0.1 and 0.5.
- h / H is between 0.2 and 0.3, and preferably between 0.23 and 0.27.
- the separation efficiency of U03 particles gases is optimal. Indeed, for a h / H ratio of less than 0.1 or even 0.2, a part of the U03 particles can be directly entrained in the filter. This results in a decrease in the separation efficiency and a sharp increase in the risk of clogging of the filter. For a h / H ratio greater than 0.5 or even 0.3, it is the thermal stresses on the walls of the separation chamber that become significant, which can then cause damage to the latter.
- the means for deflecting the gas can be provided by a partial housing of the reaction chamber in the separation chamber, the mouth of the reaction chamber in the separation chamber defining the settling location.
- the gas deflecting means may include a deflecting wall separating the mouth of the reaction chamber from the gas outlet, the lower end of said deflecting wall defining the settling location.
- An installation according to the invention comprising such a deflection means is particularly advantageous for allowing maintenance of the separation chamber without its separation efficiency being affected. Indeed, the separation chamber has no area whose access would be limited by the presence of the separation chamber.
- the side walls of the separation chamber may have only wall sections forming an angle with the vertical which is less than 60 °, preferably 45 °.
- the filter is advantageously made of a material allowing filtration in an environment whose temperature is greater than or equal to 300 ° C.
- the filter can thus be a filter comprising a material such as a wire cloth or be a filter type candle ceramic or sintered metal.
- the filter may advantageously be a sintered metal type filter.
- the burner and the reaction chamber may be configured to provide, at the outlet of the reaction chamber, a gas velocity of between 1 m / s and 2 m / s and, advantageously, between 1.4 m / s and 1, 7 m / s.
- the installation may comprise at least two sintered metal type filters connected in parallel, the installation preferably comprising four sintered metal type filters connected in parallel.
- the invention relates, secondly, to a use of an installation for thermal denitration of a hydrated uranyl nitrate corresponding to the formula ⁇ 2 ( ⁇ 3) 2, ⁇ 2 0 with 2 x x 6 6.
- the installation whose use is the subject of the invention is the installation as defined above, the advantageous features of this installation can be taken alone or in combination.
- the uranyl nitrate hydrate may be uranyl nitrate hexahydrate of formula UO2 (NO3) 2,6H20.
- the invention relates, thirdly, to a thermal denitration process of a uranyl nitrate hydrate having the formula U02 (NO3) 2, xH20 with 2 ⁇ x ⁇ 6.
- this method comprises:
- a filtration step for separating the other part of the U03 particles from said gases and thus purifying said gases, said step being carried out at a temperature greater than or equal to 350 ° C, and
- This method also makes it possible to overcome all the disadvantages associated with the pressure drop generated by the overloading of the bag filter 12 described in document [2].
- the inventors have also observed that, unexpectedly and surprisingly, the UO3 particles collected at the outlet of the settling chamber exhibit morphological characteristics that are much greater than those of the UO3 particles collected by means of the process described in the document [2].
- Such a method is particularly adapted to be implemented by means of an installation according to the invention.
- the step of separating part of the U03 particles from the gases may comprise the following substeps:
- the gases resulting from the thermal denitration can be introduced into the separation chamber with a gas velocity of between 1 m / s and 2 m / s and, advantageously, between 1.4 m / s and 1.7 m / s.
- the invention relates, fourthly, to UO3 particles. According to the invention, these particles are obtained directly by the process as described above, the advantageous characteristics of this process can be taken alone or in combination, the UO3 particles having the following characteristics:
- Such UO3 particles have a reactivity that is perfectly adapted for their subsequent conversion into uranium dioxide UO 2 and uranium tetrafluoride UF 4 .
- the BET specific surface area of the UO3 particles is between 17 m 2 / g and 21.5 m 2 / g, advantageously between 17.5 m 2 / g and 21 m 2 / g and preferably between 18 m 2 / g and 20 m 2 / g.
- FIG. 1 schematically illustrates the installation described for the implementation of the process for obtaining uranium trioxide UO3 by thermal denitration of uranyl nitrate taught by document [2].
- FIG. 2 illustrates a thermal denitration plant of hydrated uranyl nitrate according to the invention in a sectional view along the axis A-A of FIG. 3.
- FIG. 3 illustrates a view from above of an installation according to the invention in which a single filter is mounted on the four filters of the installation and in which the manhole is not closed.
- Figures 4a and 4b schematically illustrate two alternative arrangements of the reaction chamber and the separation chamber for an installation according to the invention.
- FIG. 2 illustrates a plant 1 according to the invention for carrying out a thermal denitration of a hydrated uranyl nitrate corresponding to the formula ⁇ 2 ( ⁇ 3) 2, ⁇ 2 0 with 2 x x 6 6, in uranium trioxide UO3 .
- Such an installation 1 comprises:
- reaction chamber 110 disposed at the outlet of the burner 114 and having a hydrated uranyl nitrate inlet, said reaction chamber 110 and the burner being configured to perform thermal denitration of the uranyl nitrate hydrate and form uranium trioxide UO3 being in the form of particles, a separation chamber 120 adapted to separate a portion of the U03 particles from the gases resulting from the thermal denitration carried out in the reaction chamber 110, the separation chamber 120 being a settling chamber, and
- each of these filters 130 being connected to an outlet of the gases 131 of the separation chamber 120.
- the burner 114 and the reaction chamber 110 are in accordance with the burner 4 and the reaction chamber 1 described in document [2], with the difference that the reaction chamber 110 opens directly into the separation chamber 120. Thus, it is not provided for the present pipe 1 installation 9 connecting the reaction chamber 110 to the separation chamber 120.
- the reaction chamber 110 has no end extended by a cone reducing the outlet section.
- the burner 114 comprises:
- a line 117 for supplying hydrated uranyl nitrate said line 117 being connected to the inlet of the reaction chamber 110,
- the outlet of the burner 114 is connected to the reaction chamber 110.
- the latter comprises an inlet cone through which the combustion gases and the hydrated uranyl nitrate 117, a cylindrical envelope and an outlet 113 are introduced.
- the outlet 113 of the reaction chamber 110 extends the cylindrical envelope with a cross section, that is to say substantially constant.
- the outlet 113 of the reaction chamber 110, or mouthpiece, opens directly into the separation chamber 120.
- the reaction chamber 110 is partly housed in the separation chamber 120. In this way, the reaction chamber 110 opens into the separation chamber 120 at a lower vertical dimension than that of the gas outlet 131 of the filters 130.
- the burner 114 and the reaction chamber 110 are configured to provide, at the outlet of the reaction chamber 110, a gas velocity of between 1 m / s and 2 m / s and, advantageously, between 1.4 m / s and 1.7 m / s.
- the mouth 113 of the reaction chamber 110 defines a settling location 121 in the separation chamber 120.
- gases and U03 particles leave the reaction chamber 110 after the thermal denitration reaction, they are
- the vertical dimension of the settling place 121 corresponds, as illustrated in FIG. 2, to the vertical dimension of the mouth 113 of the reaction chamber 110.
- Such a partial housing of the reaction chamber 110 in the separation chamber 120 forms a deflection means for deflecting the gases and the UO3 particles at the settling location 121.
- the separation chamber 120 has, as shown in Figures 2 and 3, a circular horizontal section and a triangular vertical section. In this way, the separation chamber 120 has a generally conical shape with the apex facing downwards.
- the side walls 122 of the separation chamber 120 have an angle vis-à-vis the vertical which is between 0 ° and 45 °.
- the side walls 122 of the separation chamber 120 therefore have only wall sections forming an angle with the vertical which is less than 60 °, and more particularly 45 °.
- the side wall 122 at the mouth 113 has an angle relative to the vertical which is close to 0 °. This eliminates the deposits of particles that could take place on the side walls 122 of the separation chamber 120.
- the lower part of the separation chamber 120 comprises, as shown in FIG. 2, an output of particles 123 for recovering the U03 particles after their separation from the gases.
- the upper part of the separation chamber 120 comprises, as illustrated in FIG. 3, four gas outlets 131 each equipped with a filter 130 for evacuating the gases after their separation from the particles.
- the outputs of each of the gases 131 defines a vertical gas outlet dimension.
- the outputs of the gases 131 define the same vertical gas outlet dimension, which corresponds to the vertical dimension of the gas outlet.
- the vertical dimension of the gas outlet corresponds, of course, to the lowest vertical output of the gases.
- the vertical dimension of the gas outlet 131 is greater than that of the mouth 113 of the reaction chamber 110 by a height h.
- the upper part of the separation chamber 120 can also be provided, as illustrated in FIG. 2, with a manhole 140 to allow inspection and maintenance of the separation chamber 120.
- the separation chamber 120 has a height H.
- This height H of the separation chamber 120 is defined in relation to the height h which corresponds to the difference in vertical dimension between the settling location 121 and that of the outlet of the gases 131. from a height h.
- the ratio h to H denoted h / H, is between 0.1 and 0.5, advantageously between 0.2 and 0.3, and preferably between 0.23 and 0.27.
- the h / H ratio is set at 0.25.
- the separation chamber 120 may have a maximum lateral dimension of between 3 m and 8 m, advantageously between 4.5 m and 6.5 m.
- the height H of the separation chamber 120 may be between 5 m and 12 m, preferably between 6 m and 9 m.
- the filters 130 are sintered metal type filters, as illustrated in FIGS. 2 and 3, a single filter 130 being shown in FIG. 3, three of the outputs of the gases 131 being shown without a filter 130. These filters make it possible to separate the Another part of the U03 particles from the gases, particles that were not particles during the separation by settling. In doing so, the gases are purified.
- each filter 130 may have a diameter of between 0.7 m and 1.7 m, preferably between 1.0 m and 1.4 m.
- the installation comprises four filters 130
- the installation comprises a different number of filters.
- the installation can be equipped as a variant with only two filters 130, or even a single filter or six filters, as long as these or the latter are suitably sized.
- the arrangement of the filters 130 as described in this embodiment is perfectly compatible with these variants if the distribution of the filters on the upper part of the separation chamber 120 is adapted to the number of filters present.
- FIGS. 4a and 4b schematically illustrate two other possible arrangements between the reaction chamber 110 and the separation chamber 120 for an installation 1 according to the invention.
- An installation 1 according to the first variant shown diagrammatically in FIG. 4a differs from the installation illustrated in FIG. 2 in that the reaction chamber 110 is not housed in the separation chamber 120, with nevertheless a mouth 113 of the chamber 110 in the separation chamber 120 whose vertical dimension remains lower than that of the gas outlet 131.
- the 120 has a portion of its upper part, the one accommodating the mouth 113 of the reaction chamber 110, lowered relative to the remainder of the upper part which accommodates the filters 130.
- Such a lowering of a portion of the upper part of the separation chamber 120 forms a deflection means for diverting gases and particles to the settling location 121. Indeed, in this first variant, it is this lowering which makes it possible to position the mouth 113 of the reaction chamber 110, and thus the settling location 121, in the separation chamber 120 with respect to the gas outlet. 131.
- An installation 1 according to the second variant is shown schematically in Figure 4b.
- Such an installation 1 differs from the installation 1 illustrated in FIG. 3 in that the reaction chamber 110 opens into the separation chamber 120 at substantially the same vertical dimension as the exit of the gases 131 and in that it is provided a deflection wall 124 separating the mouth 113 from the reaction chamber 110 in the separation chamber 120 of the gas outlet 131.
- the lower end of the deflection wall 124 defines the settling location 121 and allows divert the gases and particles leaving the mouth 113 of the reaction chamber 110 to the settling location 121.
- the deflection wall 124 forms a deflection means for deflecting the gases and the particles at the decantation location 121.
- An installation 1 according to the invention can be implemented to carry out a method of thermal denitration of a uranyl nitrate hydrate having the formula U0 2 (NO 3 ) 2, xH 2 0 with 2 x x 6 6 in order to obtain particles of U0 3 .
- Such a method comprises:
- a filtration step for separating the other part of the U03 particles from said gases and thus purifying said gases, said step being carried out at a temperature greater than or equal to 350 ° C .;
- the step of the U03 particle separation step comprises the following substeps:
- the first synthesis denoted SI, was performed in a comparative installation, in accordance with the teaching of document [2] and illustrated in FIG.
- the second synthesis denoted S2 was carried out in an installation according to the invention and illustrated in FIGS. 2 and 3.
- the burner 4, 114 ensures the combustion of natural gas in the supercharged air by excitation of a spark plug not shown in FIGS. 1 to 3.
- the combustion being entirely carried out in the burner 4, 114, the nitrate of uranyl hexahydrate injected is never in contact with the flame.
- the gases resulting from the combustion a temperature of about 1400 ° C, are accelerated in the burner 4, 114 to reach a speed of about 300 m / s in the upper conical portion of the reaction chamber 1, 110 or reaction zone in which the hot combustion gases and the uranyl nitrate hexahydrate sprayed into fine droplets are brought into contact.
- the U03 particles obtained at the end of the first synthesis S1 were collected, on the one hand by the pipe 10 and on the other hand by the pipe 13.
- the U03 particles obtained at the end of the second synthesis S2 were collected by the single outlet 123 of the settling chamber 120.
- Table 1 The ranges of specific surface values and mass percentages of water and NO 3 - as obtained over several tests are given in Table 1. Below, Table 1 also shows the U03 particle collection efficiencies. .
- the U03 particles as obtained by the implementation of the thermal denitration process in an installation according to the invention therefore have a BET specific surface area which is greater than that of the mixture of UO3 particles collected by lines 10 and 13.
- the U03 particles obtained by the second synthesis S2 have very low levels of contamination of water and nitrate ions, respectively less than 0.4% m and 0.7% m. Such percentages further favor the reactivity of the UO3 particles for their subsequent conversion into U0 2 and then to UF 4 .
- the purified gases were sucked out of the filters 130 by means of fans providing a suction flow rate of 185 kg / h, which is much lower. than the previous one, and this, in the absence of additional cooling device.
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Abstract
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CN201680034147.XA CN107771163B (zh) | 2015-06-12 | 2016-06-10 | 热脱硝用设备和方法、该设备的应用及该方法获得的产品 |
RU2018100791A RU2701921C2 (ru) | 2015-06-12 | 2016-06-10 | Устройство и способ термического деазотирования, применение такого устройства и продукт, полученный таким способом |
GB1801213.8A GB2556739B (en) | 2015-06-12 | 2016-06-10 | Apparatus and process for thermal denitration, use of such an apparatus and product obtained by means of such a process |
AU2016275707A AU2016275707B2 (en) | 2015-06-12 | 2016-06-10 | Apparatus and process for thermal denitration, use of such an apparatus and product obtained by means of such a process |
GBGB1720461.1A GB201720461D0 (en) | 2015-06-12 | 2016-06-10 | Apparatus and process for thermal dentration, use of such an apparatus and product obtained by means of such a process |
JP2017564433A JP6921004B2 (ja) | 2015-06-12 | 2016-06-10 | 熱的脱硝のための装置及び方法、そのような装置の使用、及びそのような方法を用いて得られた生成物 |
CA2988359A CA2988359C (fr) | 2015-06-12 | 2016-06-10 | Installation, procede de denitration thermique, utilisation d'une telle installation et produit obtenu par un tel procede |
US15/735,441 US11440809B2 (en) | 2015-06-12 | 2016-06-10 | Apparatus and process for thermal denitration, use of such an apparatus and product obtained by means of such a process |
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FR1555380A FR3037331B1 (fr) | 2015-06-12 | 2015-06-12 | Installation, procede de denitration thermique, utilisation d'une telle installation et produit obtenu par un tel procede |
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US (1) | US11440809B2 (fr) |
JP (1) | JP6921004B2 (fr) |
CN (1) | CN107771163B (fr) |
AU (1) | AU2016275707B2 (fr) |
CA (1) | CA2988359C (fr) |
FR (1) | FR3037331B1 (fr) |
GB (2) | GB2556739B (fr) |
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FR3061165B1 (fr) | 2016-12-22 | 2019-09-13 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Structure microelectronique a amortissement visqueux controle par maitrise de l'effet thermo-piezoresistif |
US20210398699A1 (en) * | 2018-10-09 | 2021-12-23 | Framatome | Method and facility for converting uranium hexafluoride into uranium dioxide |
CN109607610A (zh) * | 2018-11-19 | 2019-04-12 | 中核二七二铀业有限责任公司 | 一种硝酸铪热脱硝制备二氧化铪的方法 |
CN114644359A (zh) * | 2020-12-18 | 2022-06-21 | 中核四0四有限公司 | 一种使用天然气进行硝酸铀酰热解脱硝制备uo3的方法 |
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US2981592A (en) * | 1957-05-13 | 1961-04-25 | Lawroski Stephen | Method and apparatus for calcining salt solutions |
WO1984002124A1 (fr) | 1982-11-30 | 1984-06-07 | Comurhex | Procede d'obtention de uo3 de grande reactivite par decomposition thermique sous forme solide de nitrate d'uranyle hydrate |
US5628048A (en) | 1994-06-13 | 1997-05-06 | Comurhex Societe Pour La Conversion De L'uranium En Metal Et Hexafluorure | Process for obtaining uranium trioxide by direct thermal denitration of uranyl nitrate |
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US2755853A (en) * | 1954-11-10 | 1956-07-24 | Ronald S Edgett | Denitration apparatus |
GB928861A (fr) * | 1960-04-08 | |||
JPS6045934B2 (ja) * | 1980-07-18 | 1985-10-12 | 三菱マテリアル株式会社 | 流動層反応塔用固気分離装置 |
FR2526006A1 (fr) * | 1982-04-30 | 1983-11-04 | Comurhex | Procede d'obtention de uo3 de grande surface specifique a partir de nitrate d'uranyle hydrate |
JPS58194742A (ja) * | 1982-05-04 | 1983-11-12 | Toshiba Corp | ウランの脱硝処理方法 |
FR2555566B1 (fr) * | 1983-11-25 | 1989-02-17 | Comurhex | Procede de preparation d'oxydes metalliques pulverulents a partir de solutions aqueuses ou de melanges solides de nitrates metalliques |
KR900003608B1 (ko) * | 1987-09-30 | 1990-05-26 | 한국에너지연구소 | 도토리와 오배자를 이용한 우라늄 회수 방법 |
FR2742254B1 (fr) * | 1995-12-12 | 1998-02-13 | Comurhex | Procede d'obtention d'un melange d'oxydes metalliques pulverulents, appartenant a la filiere nucleaire, a partir de leurs nitrates |
US7731912B2 (en) * | 2006-09-14 | 2010-06-08 | Atomic Energy Of Canada Limited | Evaporator/calciner |
CN101891253B (zh) * | 2010-07-16 | 2012-08-22 | 中国原子能科学研究院 | 单分散微米级铀氧化物微粒的制备方法 |
CN103910385B (zh) * | 2013-01-08 | 2015-08-26 | 中核四0四有限公司 | 脱硝三氧化铀水合活化工艺 |
US9511339B2 (en) * | 2013-08-30 | 2016-12-06 | Honeywell International Inc. | Series coupled fluidized bed reactor units including cyclonic plenum assemblies and related methods of hydrofluorination |
CN206266242U (zh) * | 2016-10-09 | 2017-06-20 | 靖江市国润干燥设备有限公司 | 一种使用喷雾干燥技术处理硝酸铀酰热解脱销的设备 |
CN107162060A (zh) * | 2017-05-26 | 2017-09-15 | 中核四0四有限公司 | 一种硝酸铀酰气流式雾化干燥热解脱硝制备uo3工艺 |
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2015
- 2015-06-12 FR FR1555380A patent/FR3037331B1/fr active Active
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2016
- 2016-06-10 JP JP2017564433A patent/JP6921004B2/ja active Active
- 2016-06-10 GB GB1801213.8A patent/GB2556739B/en active Active
- 2016-06-10 CN CN201680034147.XA patent/CN107771163B/zh active Active
- 2016-06-10 RU RU2018100791A patent/RU2701921C2/ru active
- 2016-06-10 AU AU2016275707A patent/AU2016275707B2/en active Active
- 2016-06-10 GB GBGB1720461.1A patent/GB201720461D0/en active Pending
- 2016-06-10 US US15/735,441 patent/US11440809B2/en active Active
- 2016-06-10 WO PCT/EP2016/063377 patent/WO2016198654A1/fr active Application Filing
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Patent Citations (3)
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US2981592A (en) * | 1957-05-13 | 1961-04-25 | Lawroski Stephen | Method and apparatus for calcining salt solutions |
WO1984002124A1 (fr) | 1982-11-30 | 1984-06-07 | Comurhex | Procede d'obtention de uo3 de grande reactivite par decomposition thermique sous forme solide de nitrate d'uranyle hydrate |
US5628048A (en) | 1994-06-13 | 1997-05-06 | Comurhex Societe Pour La Conversion De L'uranium En Metal Et Hexafluorure | Process for obtaining uranium trioxide by direct thermal denitration of uranyl nitrate |
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JP6921004B2 (ja) | 2021-08-18 |
CN107771163A (zh) | 2018-03-06 |
RU2018100791A (ru) | 2019-07-12 |
FR3037331A1 (fr) | 2016-12-16 |
AU2016275707A1 (en) | 2018-01-04 |
CN107771163B (zh) | 2020-02-21 |
GB2556739A (en) | 2018-06-06 |
RU2018100791A3 (fr) | 2019-07-24 |
US20180179081A1 (en) | 2018-06-28 |
US11440809B2 (en) | 2022-09-13 |
JP2018526307A (ja) | 2018-09-13 |
GB201720461D0 (en) | 2018-01-24 |
CA2988359C (fr) | 2023-09-12 |
GB2556739B (en) | 2022-04-20 |
AU2016275707B2 (en) | 2019-08-29 |
RU2701921C2 (ru) | 2019-10-02 |
FR3037331B1 (fr) | 2019-09-13 |
GB201801213D0 (en) | 2018-03-14 |
CA2988359A1 (fr) | 2016-12-15 |
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