JP3183314B2 - Production equipment for uranyl fluoride powder - Google Patents
Production equipment for uranyl fluoride powderInfo
- Publication number
- JP3183314B2 JP3183314B2 JP02011093A JP2011093A JP3183314B2 JP 3183314 B2 JP3183314 B2 JP 3183314B2 JP 02011093 A JP02011093 A JP 02011093A JP 2011093 A JP2011093 A JP 2011093A JP 3183314 B2 JP3183314 B2 JP 3183314B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- reaction tower
- uranyl fluoride
- gas
- fluoride powder
- 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.)
- Expired - Fee Related
Links
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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- 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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、六フッ化ウランからフ
ッ化ウラニル粉末を製造する装置に関する。更に詳しく
は、流動層において六フッ化ウランを高温で加水分解し
てフッ化ウラニル粉末を製造する装置に関するものであ
る。The present invention relates to an apparatus for producing uranyl fluoride powder from uranium hexafluoride. More specifically, the present invention relates to an apparatus for producing uranyl fluoride powder by hydrolyzing uranium hexafluoride at a high temperature in a fluidized bed.
【０００２】[0002]
【従来の技術】この種の製造装置は、六フッ化ウランか
ら核燃料に適した二酸化ウランを製造する一連のプロセ
スの中の一装置として用いられる。従来、六フッ化ウラ
ンを高温で加水分解する反応装置として、傾斜回転バレ
ル型キルン装置、噴霧火炎反応装置、流動層反応装置等
が知られている。傾斜回転バレル型キルン装置では、例
えば特公昭５１−１６９１５号公報に開示されているよ
うに、傾斜して回転するキルン胴部の上端に接続して設
けられた入口室の中で六フッ化ウラン蒸気と乾燥水蒸気
とが噴射ノズルから一緒に噴射される。噴射と同時に六
フッ化ウランが水蒸気により加水分解されフッ化ウラニ
ル粉末になり、この粉末がキルン胴部の上端から下端に
ゆっくりと移動する。下端に向うフッ化ウラニル粉末は
キルン胴部の下端から供給される水蒸気、水素又は水蒸
気／水素混合物に接触して酸化ウランとなる。2. Description of the Related Art A production apparatus of this kind is used as an apparatus in a series of processes for producing uranium dioxide suitable for nuclear fuel from uranium hexafluoride. Conventionally, as a reactor for hydrolyzing uranium hexafluoride at a high temperature, an inclined rotary barrel kiln, a spray flame reactor, a fluidized bed reactor, and the like are known. In an inclined rotary barrel type kiln apparatus, as disclosed in, for example, Japanese Patent Publication No. 51-16915, uranium hexafluoride is contained in an inlet chamber provided at the upper end of a kiln body which rotates in an inclined manner. Steam and dry steam are injected together from the injection nozzle. Simultaneously with the injection, uranium hexafluoride is hydrolyzed by water vapor into uranyl fluoride powder, which slowly moves from the upper end to the lower end of the kiln body. The uranyl fluoride powder toward the lower end comes into contact with water vapor, hydrogen or a water vapor / hydrogen mixture supplied from the lower end of the kiln body to become uranium oxide.
【０００３】噴霧火炎反応装置では、例えば特公昭５９
−４５６０５号公報に開示されているように、水素、酸
素、水蒸気などにより構成される炎（フレーム）の中に
六フッ化ウランを酸素及び還元性ガスとともに供給し
て、これらを高温で反応させてフッ素を含むウラン酸化
物を得ている。流動層反応装置では、例えば米国特許第
４，０５３，５５９号の明細書に開示されているよう
に、水蒸気により流動化しているフッ化ウラニル粒子の
層の中に六フッ化ウランガスを供給して、反応により生
成したフッ化ウラニル粉末を流動層を形成しているフッ
化ウラニル粒子の表面に析出させ、これを抜出してい
る。上記噴霧火炎反応装置及び流動層反応装置で得られ
たフッ素を含むウラン酸化物は、更に別の流動層反応装
置等で水蒸気と高温で反応してフッ素をほとんど含まな
い酸化ウランに変換できることが知られている。[0003] In the spray flame reactor, for example,
As disclosed in Japanese Patent No. 45605, uranium hexafluoride is supplied together with oxygen and a reducing gas into a flame (flame) composed of hydrogen, oxygen, water vapor, etc., and reacted at a high temperature. To obtain a uranium oxide containing fluorine. In a fluidized bed reactor, uranium hexafluoride gas is supplied into a bed of uranyl fluoride particles fluidized by steam as disclosed in, for example, the specification of US Pat. No. 4,053,559. The uranyl fluoride powder produced by the reaction is precipitated on the surface of the uranyl fluoride particles forming the fluidized bed, and is extracted. It is known that uranium oxide containing fluorine obtained by the above spray flame reactor and fluidized bed reactor can be converted into uranium oxide containing almost no fluorine by reacting with steam at a high temperature in another fluidized bed reactor or the like. Have been.
【０００４】[0004]
【発明が解決しようとする課題】しかし、上記傾斜回転
バレル型キルン装置及び噴霧火炎反応装置で得られたフ
ッ化ウラニル粉末は、水蒸気と六フッ化ウランとが気相
で反応して生成される一次粒子の凝集体である。このた
め、得られたフッ化ウラニル粉末は、平均粒径が１μｍ
以下で小さく、形状も不規則である。また凝集体である
ため粉末にポアが多く崩れ易い。この結果、粉末として
の取扱いが難しい問題点があった。一方、流動層反応装
置で得られたフッ化ウラニル粉末は、流動化しているフ
ッ化ウラニル粒子の表面にフッ化ウラニル粉末を繰返し
析出して作られるために、高密度で球形状に近い粉末に
なり、更に流動性にも優れる。しかしこの造粒の原理か
らも明らかなように、この装置では流動層内のフッ化ウ
ラニル粉末は時間の経過とともに粒径が大きくなる一方
で、細かい粉末を供給しなければ流動層を維持すること
ができない。従来、流動層反応装置でこの細かい粉末を
供給する方法として、得られた粉末の一部を粉砕して流
動層の中に戻したり、或いは流動層の中に内部粉砕機構
を設けたりしていた。しかし、これらの方法は粉砕手段
を反応塔の外部又は内部に備える必要があり、装置の構
成が複雑化する問題点があった。However, the uranyl fluoride powder obtained by the inclined rotary barrel type kiln and the spray flame reactor is produced by reacting water vapor and uranium hexafluoride in a gas phase. It is an aggregate of primary particles. For this reason, the obtained uranyl fluoride powder has an average particle size of 1 μm.
Below are small and irregular in shape. In addition, since the powder is an aggregate, the powder has many pores and easily collapses. As a result, there is a problem that it is difficult to handle the powder. On the other hand, the uranyl fluoride powder obtained in the fluidized bed reactor is made by repeatedly depositing the uranyl fluoride powder on the surface of the fluidized uranyl fluoride particles. And also have excellent fluidity. However, as is clear from the principle of this granulation, in this apparatus, the particle size of the uranyl fluoride powder in the fluidized bed increases with the passage of time, but the fluidized bed must be maintained unless fine powder is supplied. Can not. Conventionally, as a method of supplying this fine powder in a fluidized bed reactor, a part of the obtained powder was pulverized and returned into the fluidized bed, or an internal pulverizing mechanism was provided in the fluidized bed. . However, in these methods, it is necessary to provide the pulverizing means outside or inside the reaction tower, and there is a problem that the configuration of the apparatus is complicated.
【０００５】本発明の目的は、反応塔の外部又は内部に
粉末の粉砕手段を備えることなく流動層内で細かい粉末
を生成することにより、取扱いが容易で流動性に優れた
フッ化ウラニル粉末を連続して製造する装置を提供する
ことにある。本発明の別の目的は、流動層を形成するフ
ッ化ウラニル粉末の平均粒径や粒度分布を任意に調整
し、かつ調整したフッ化ウラニル粉末を得るフッ化ウラ
ニル粉末の製造装置を提供することにある。An object of the present invention is to produce uranyl fluoride powder which is easy to handle and has excellent fluidity by producing fine powder in a fluidized bed without providing a means for pulverizing the powder outside or inside the reaction tower. An object of the present invention is to provide an apparatus for continuously manufacturing. Another object of the present invention is to provide an apparatus for producing a uranyl fluoride powder which arbitrarily adjusts the average particle size and particle size distribution of the uranyl fluoride powder forming the fluidized bed, and obtains the adjusted uranyl fluoride powder. It is in.
【０００６】[0006]
【課題を解決するための手段】上記目的を達成するため
の本発明の構成を実施例に対応する図１に基づいて説明
する。本発明は、反応塔１０内に形成され六フッ化ウラ
ンを水蒸気により高温で加水分解する流動層１２と、反
応塔１０に六フッ化ウランを供給する供給ノズル２５
と、反応塔１０の底部に設けられ水蒸気を流動層１２に
向けて噴出するガス噴出部１４と、反応塔１０の上部に
設けられ加水分解により生成して上昇するフッ化水素ガ
スと加水分解により生成し前記ガスに同伴して浮上する
フッ化ウラニル粉末とを分離する固気分離部１８と、流
動層１２の表面部近傍の反応塔１０に設けられその表面
部で生成されたフッ化ウラニル粉末を抜出す上部抜出し
部１７と、流動層１２の深部近傍の反応塔１０に設けら
れ深部で生成されたフッ化ウラニル粉末を抜出す下部抜
出し部１６とを備えたフッ化ウラニル粉末の製造装置の
改良である。その特徴ある点は、供給ノズル２５が流動
層１２の表面部に相応する位置の反応塔１０に設けられ
た第１供給ノズル２６と、流動層１２の深部に相応する
位置の反応塔１０に設けられた第２供給ノズル２７とに
より構成されたことにある。なお、第１供給ノズル２６
に接続された六フッ化ウラン第１供給管２６ａに第１流
量調整弁２６ｂを設け、第２供給ノズル２７に接続され
た六フッ化ウラン第２供給管２７ａに第２流量調整弁２
７ｂを設け、第１流量調整弁２６ｂと第２流量調整弁２
７ｂとをコントローラ３０により互いに独立して制御す
ることが好ましい。A configuration of the present invention for achieving the above object will be described with reference to FIG. 1 corresponding to an embodiment. The present invention includes a fluidized bed 12 formed in the reaction tower 10 for hydrolyzing uranium hexafluoride with steam at a high temperature, and a supply nozzle 25 for supplying uranium hexafluoride to the reaction tower 10.
A gas jetting portion 14 provided at the bottom of the reaction tower 10 for jetting water vapor toward the fluidized bed 12, and a hydrogen fluoride gas provided at the top of the reaction tower 10, which is generated by hydrolysis and rises by hydrolysis. A solid-gas separation section 18 for separating the uranyl fluoride powder generated and floating with the gas, and a uranyl fluoride powder provided in the reaction tower 10 near the surface of the fluidized bed 12 and generated on the surface thereof Of a uranyl fluoride powder production apparatus, comprising: an upper extraction section 17 for extracting water; and a lower extraction section 16 provided in the reaction tower 10 near the deep part of the fluidized bed 12 and for extracting uranyl fluoride powder generated in the deep part. It is an improvement. The characteristic point is that the supply nozzle 25 is provided in the first supply nozzle 26 provided at the position corresponding to the surface portion of the fluidized bed 12 and the reaction nozzle 10 provided at the position corresponding to the deep portion of the fluidized bed 12. And the second supply nozzle 27 provided. The first supply nozzle 26
The first flow control valve 26b is provided in the first uranium hexafluoride supply pipe 26a connected to the second supply nozzle 27, and the second flow control valve 2 is provided in the second uranium hexafluoride supply pipe 27a connected to the second supply nozzle 27.
7b, the first flow control valve 26b and the second flow control valve 2
7b are preferably controlled independently of each other by the controller 30.
【０００７】[0007]
【作用】第１及び第２供給ノズル２６，２７から供給さ
れた六フッ化ウランはそれぞれ次の式（１）に示すよう
にガス噴出部１４から供給された水蒸気と反応してフッ
化ウラニル粉末とフッ化水素ガスを生成する。 ＵＦ6 ＋ ２Ｈ2Ｏ → ＵＯ2Ｆ2 ＋ ４ＨＦ ↑ ・・・（１） 第２供給ノズル２７から供給された六フッ化ウランは、
流動層内のフッ化ウラニル粒子の表面に付着してこの粒
径を増大するように作用する。一方、第１供給ノズル２
６から供給された六フッ化ウランは、生成したフッ化ウ
ラニル粉末同士が結合した凝集体の形態になり易い。こ
のフッ化ウラニル粉末は、既に流動層を形成していた粉
末と比較すると粒径が小さい。流動層を攪拌する流動用
ガスの作用により、層表面部の粉末と層深部の粉末が均
一に混合され、特別な粉砕手段を設けなくても流動層１
２に細かいフッ化ウラニル粉末が連続して供給される。The uranium hexafluoride supplied from the first and second supply nozzles 26 and 27 reacts with the water vapor supplied from the gas jetting section 14 as shown in the following equation (1) to produce uranyl fluoride powder. And hydrogen fluoride gas. UF 6 + 2H 2 O → UO 2 F 2 + 4HF ↑ (1) The uranium hexafluoride supplied from the second supply nozzle 27 is
It adheres to the surface of the uranyl fluoride particles in the fluidized bed and acts to increase the particle size. On the other hand, the first supply nozzle 2
The uranium hexafluoride supplied from 6 tends to be in the form of an aggregate in which the generated uranyl fluoride powders are bonded to each other. The uranyl fluoride powder has a smaller particle size as compared with the powder that has already formed a fluidized bed. By the action of the fluidizing gas that stirs the fluidized bed, the powder on the surface of the bed and the powder on the deeper part of the bed are mixed uniformly, and the fluidized bed 1 can be prepared without any special pulverizing means.
2, fine uranyl fluoride powder is continuously supplied.
【０００８】[0008]
【実施例】以下、本発明の一実施例を図面に基づいて詳
しく説明する。図１に示すように、反応塔１０の内底部
近傍には分散板１１が反応塔１０の内部を区画するよう
に設けられる。この分散板１１より上の反応塔内部には
六フッ化ウランを水蒸気により高温で加水分解する流動
層１２が形成される。流動層１２はフッ化ウラニル粒子
からなるシード粉により構成される。分散板１１はこの
例では多孔質のメッシュに形成され、流動用ガスは透過
するが、シード粉は抜け落ちないようになっている。ま
た分散板１１より下の反応塔内部には上記流動層１２を
流動状態にするためのガス噴出区域１３が形成される。
反応塔１０の底部側壁にはこのガス噴出区域内に向けて
水蒸気を噴出するガス噴出管１４が設けられ、ガス噴出
管１４には開閉弁１４ａが設けられる。流動層１２はガ
ス噴出管１４及びガス噴出区域１３を通って分散板１１
を透過する水蒸気により流動状態になる。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below in detail with reference to the drawings. As shown in FIG. 1, a dispersion plate 11 is provided near the inner bottom of the reaction tower 10 so as to partition the inside of the reaction tower 10. A fluidized bed 12 for hydrolyzing uranium hexafluoride at high temperature with steam is formed inside the reaction tower above the dispersion plate 11. The fluidized bed 12 is composed of seed powder composed of uranyl fluoride particles. In this example, the dispersing plate 11 is formed in a porous mesh so that the flowing gas is permeable but the seed powder does not fall off. Further, a gas ejection area 13 for forming the fluidized bed 12 in a fluidized state is formed inside the reaction tower below the dispersion plate 11.
On the bottom side wall of the reaction tower 10, a gas ejection pipe 14 for ejecting water vapor into the gas ejection area is provided, and the gas ejection pipe 14 is provided with an on-off valve 14a. The fluidized bed 12 passes through the gas discharge pipe 14 and the gas discharge area 13 and
Into a fluidized state due to the water vapor passing through.
【０００９】流動層１２の深部にあるフッ化ウラニル粉
末を反応塔１０の外部に抜き出す下部抜出し管１６が分
散板１１及び反応塔１０の底部を貫通して設けられる。
また流動層１２の表面部にあるフッ化ウラニル粉末を反
応塔１０の外部に抜き出す上部抜出し管１７が反応塔１
０の側壁を貫通して設けられる。下部抜出し管１６には
開閉弁１６ａが設けられる。反応塔１０の上部には加水
分解により生成して上昇するフッ化水素ガスと加水分解
により生成し前記ガスに同伴して浮上するフッ化ウラニ
ル粉末とを分離する固気分離フィルタ１８が設けられ
る。フィルタ１８の上部には反応塔の上部を区画する区
画板１９が設けられ、この区画板１９で形成された排気
区域２１に連通してオフガス管２２が反応塔１０を貫通
して設けられる。このオフガス管２２はオフガスコレク
タ２３の凝縮器２３ａを介して凝縮液受槽２３ｂに接続
される。固気分離フィルタ１８の上端には逆洗用の不活
性ガスを吹込む逆洗管２４が接続され、逆洗管２４には
逆洗弁２４ａが設けられる。この例では不活性ガスは窒
素である。３０はコントローラであって、その出力はガ
ス噴出管１４の開閉弁１４ａ，下部抜出し管１６の開閉
弁１６ａ及び逆洗管２４の逆洗弁２４ａにそれぞれ接続
される。A lower extraction pipe 16 for extracting uranyl fluoride powder located deep in the fluidized bed 12 to the outside of the reaction tower 10 is provided through the dispersion plate 11 and the bottom of the reaction tower 10.
The upper extraction pipe 17 for extracting uranyl fluoride powder on the surface of the fluidized bed 12 to the outside of the reaction tower 10 is connected to the reaction tower 1.
0 through the side wall. The lower extraction pipe 16 is provided with an on-off valve 16a. A solid-gas separation filter 18 is provided at the upper part of the reaction tower 10 for separating hydrogen fluoride gas generated by hydrolysis and rising and uranyl fluoride powder generated by hydrolysis and floating with the gas. A partition plate 19 that partitions the upper part of the reaction tower is provided above the filter 18, and an off-gas pipe 22 is provided through the reaction tower 10 so as to communicate with an exhaust area 21 formed by the partition plate 19. This off-gas pipe 22 is connected to a condensed liquid receiving tank 23b via a condenser 23a of an off-gas collector 23. A backwash tube 24 for blowing backwashing inert gas is connected to the upper end of the solid-gas separation filter 18, and the backwash tube 24 is provided with a backwash valve 24a. In this example, the inert gas is nitrogen. Reference numeral 30 denotes a controller, the output of which is connected to the on-off valve 14a of the gas ejection pipe 14, the on-off valve 16a of the lower extraction pipe 16, and the backwash valve 24a of the backwash pipe 24, respectively.
【００１０】本実施例の特徴ある点は、反応塔１０内に
六フッ化ウランを供給する供給ノズル２５が流動層１２
の表面部に相応する位置の反応塔１０に設けられた第１
供給ノズル２６と、流動層１２の深部に相応する位置の
反応塔１０に設けられた第２供給ノズル２７とにより構
成されたことにある。第１供給ノズル２６には六フッ化
ウラン第１供給管２６ａが接続され、この供給管２６ａ
には第１流量調整弁２６ｂが設けられる。また第２供給
ノズル２７には六フッ化ウラン第２供給管２７ａが接続
され、この供給管２７ａには第２流量調整弁２７ｂが設
けられる。第１流量調整弁２６ｂと第２流量調整弁２７
ｂは電磁弁であって、ともに前述のコントローラ３０の
出力が接続される。これらの流量調整弁２６ｂ，２７ｂ
はコントローラ３０により互いに独立して開閉制御され
る。The present embodiment is characterized in that a supply nozzle 25 for supplying uranium hexafluoride into the reaction tower 10 is provided with a fluidized bed 12.
The first portion provided in the reaction tower 10 at a position corresponding to the surface portion of
It is constituted by a supply nozzle 26 and a second supply nozzle 27 provided in the reaction tower 10 at a position corresponding to the deep part of the fluidized bed 12. The first supply nozzle 26 is connected to a first supply pipe 26a of uranium hexafluoride.
Is provided with a first flow control valve 26b. The second supply nozzle 27 is connected to a second supply pipe 27a of uranium hexafluoride, and the supply pipe 27a is provided with a second flow control valve 27b. First flow control valve 26b and second flow control valve 27
An electromagnetic valve b is connected to the output of the controller 30 described above. These flow control valves 26b, 27b
Are opened and closed independently of each other by the controller 30.
【００１１】このような構成のフッ化ウラニル粉末の製
造装置では、コントローラ３０により開閉弁１４ａを開
放して水蒸気(Ｈ2Ｏ)を反応塔１０内に供給すると、流
動層１２が流動状態になり、ここで流量調整弁２６ｂ，
２７ｂを開放して六フッ化ウラン(ＵＦ6)を反応塔１０
内に供給すると、供給された六フッ化ウランが分散板１
１を透過してきた水蒸気と反応してフッ化ウラニル粉末
(ＵＯ2Ｆ2)とフッ化水素ガス(ＨＦ)を生成する。流動層
の深部に置かれた第２供給ノズル２７から供給された六
フッ化ウランは、ノズル２７の近傍にあるシード粉のフ
ッ化ウラニル粒子が密に存在するために、反応により生
成したフッ化ウラニル粉末のほぼ全量が流動層内のフッ
化ウラニル粒子の表面に付着してこの粒径を増大するよ
うに作用する。これに対して流動層の表面部に置かれた
第１供給ノズル２６から供給された六フッ化ウランは、
ノズル２６の近傍のフッ化ウラニル粒子の割合が希薄で
あるために、反応により生成したフッ化ウラニル粉末が
流動層内のフッ化ウラニル粒子の表面に付着する割合が
減少し、生成したフッ化ウラニル粉末同士が結合した凝
集体の割合が増加する。この結果、ノズル２６から供給
された六フッ化ウランにより流動層に新たに形成される
フッ化ウラニル粉末は、既に流動層を形成していた粉末
と比較すると粒径が小さくなる。In the apparatus for producing uranyl fluoride powder having such a configuration, when the controller 30 opens the on-off valve 14a to supply steam (H 2 O) into the reaction tower 10, the fluidized bed 12 becomes a fluidized state. , Where the flow control valve 26b,
27b is opened and uranium hexafluoride (UF 6 ) is supplied to the reaction tower 10
Uranium hexafluoride is supplied to the dispersion plate 1
Uranyl fluoride powder reacts with water vapor that has passed through 1
(UO 2 F 2 ) and hydrogen fluoride gas (HF) are generated. The uranium hexafluoride supplied from the second supply nozzle 27 placed in the deep part of the fluidized bed contains uranium fluoride particles of the seed powder in the vicinity of the nozzle 27 densely, so that the fluorinated product generated by the reaction is generated. Almost all of the uranyl powder adheres to the surface of the uranyl fluoride particles in the fluidized bed and acts to increase the particle size. On the other hand, uranium hexafluoride supplied from the first supply nozzle 26 placed on the surface of the fluidized bed is:
Since the ratio of the uranyl fluoride particles near the nozzle 26 is low, the ratio of uranyl fluoride powder generated by the reaction to the surface of the uranyl fluoride particles in the fluidized bed decreases, and the generated uranyl fluoride particles decrease. The proportion of aggregates in which the powders are bound increases. As a result, the uranyl fluoride powder newly formed in the fluidized bed by the uranium hexafluoride supplied from the nozzle 26 has a smaller particle size than the powder that has already formed the fluidized bed.
【００１２】流動層を攪拌する流動用ガスの作用によ
り、層表面部の粉末と層深部の粉末が均一に混合され、
特別な粉砕手段を設けなくても流動層１２に細かいフッ
化ウラニル粉末が連続して供給される。上昇するフッ化
水素ガスに同伴して浮上するフッ化ウラニル微粉末は反
応塔１０の上部に設けられた固気分離フィルタ１８の周
囲に付着する。コントローラ３０は定期的に逆洗弁２４
ａを開放して不活性ガスをフィルタ１８に吹込み、付着
したフッ化ウラニル粉末を落下させ流動層１２に戻す。
フィルタ１８を通過したフッ化水素ガス及び窒素ガスは
オフガス管２２を通ってオフガスコレクタ２３の凝縮器
２３ａで凝縮され、窒素ガスは排出管２３ｃを通って排
出され、凝縮液は受槽２３ｂに貯蔵される。By the action of the fluidizing gas for stirring the fluidized bed, the powder at the surface of the bed and the powder at the depth of the bed are uniformly mixed,
The fine uranyl fluoride powder is continuously supplied to the fluidized bed 12 without providing any special grinding means. The uranyl fluoride fine powder that floats along with the rising hydrogen fluoride gas adheres to the periphery of the solid-gas separation filter 18 provided at the upper part of the reaction tower 10. The controller 30 periodically checks the backwash valve 24.
a is opened and an inert gas is blown into the filter 18 to drop the attached uranyl fluoride powder back to the fluidized bed 12.
The hydrogen fluoride gas and the nitrogen gas passing through the filter 18 pass through the off-gas pipe 22 and are condensed in the condenser 23a of the off-gas collector 23, the nitrogen gas is discharged through the discharge pipe 23c, and the condensate is stored in the receiving tank 23b. You.
【００１３】第１流量調整弁２６ａの開度を大きくすれ
ば、微小の粒径のフッ化ウラニル粉末がより多く生成さ
れ、流動層１２を形成するフッ化ウラニル粉末の平均粒
径を小さくする。反対に第２流量調整弁２７ａの開度を
大きくすれば、フッ化ウラニル粒子の造粒作用が活発に
なり、流動層１２を形成するフッ化ウラニル粉末の平均
粒径を大きくする。調整弁２６ａ，２７ａの開閉時間を
制御すれば、任意の粒度分布のフッ化ウラニル粉末を作
ることもできる。生成したフッ化ウラニル粉末の取り出
し方としては、細かい粉末がほとんど含まれないように
する場合には流動層１２の深部に近い下部抜出し管１６
から抜出すようにすればよい。また細かい粉末が含まれ
ていてもよい場合には流動層１２の表面部に近い上部抜
出し管１７から抜出すようにすればよい。If the opening of the first flow control valve 26a is increased, more uranyl fluoride powder having a fine particle diameter is generated more, and the average particle diameter of the uranyl fluoride powder forming the fluidized bed 12 is reduced. Conversely, if the opening of the second flow control valve 27a is increased, the granulating action of the uranyl fluoride particles becomes active, and the average particle size of the uranyl fluoride powder forming the fluidized bed 12 is increased. By controlling the opening and closing time of the regulating valves 26a and 27a, uranyl fluoride powder having an arbitrary particle size distribution can be produced. As a method of taking out the generated uranyl fluoride powder, in order to hardly contain a fine powder, the lower extraction pipe 16 close to the deep part of the fluidized bed 12 is used.
You should just pull it out of. In the case where fine powder may be contained, the fine powder may be extracted from the upper extraction pipe 17 close to the surface of the fluidized bed 12.
【００１４】なお、上記例では水蒸気を流動層の流動用
ガスとしたが、上記式（１）の反応に影響しない、例え
ば不活性ガスを水蒸気の外に流動用ガスとしてもよい。
また、不活性ガスとして窒素を挙げたが、アルゴン、ヘ
リウム等でもよい。更に、分散板として多孔質のメッシ
ュ構造のものを例示したが、バブルキャップトレイでも
よい。In the above example, steam is used as the fluidizing gas for the fluidized bed. However, an inert gas which does not affect the reaction of the above formula (1) may be used as the fluidizing gas in addition to the steam.
In addition, although nitrogen is mentioned as an inert gas, argon, helium or the like may be used. Further, the dispersion plate has a porous mesh structure, but may be a bubble cap tray.
【００１５】[0015]
【発明の効果】以上述べたように、本発明の製造装置に
よれば、反応塔の外部又は内部に複雑な粉砕手段を用い
ることなく、第１供給ノズルにより造粒の種になる細か
いフッ化ウラニル粉末を製造でき、この結果、取扱いが
容易で流動性に優れたフッ化ウラニル粉末を連続して製
造できる。また、第１及び第２供給ノズルに供給する六
フッ化ウランの供給割合を変化させることにより、流動
層を形成するフッ化ウラニル粉末の平均粒径や粒度分布
を比較的任意に設定することでき、生成したフッ化ウラ
ニル粉末を上部抜出し管又は下部抜出し管のいずれかか
ら抜出すことにより、所望の粒径のフッ化ウラニル粉末
が得られる。As described above, according to the production apparatus of the present invention, fine fluoridation that becomes seeds of granulation by the first supply nozzle can be performed without using complicated crushing means outside or inside the reaction tower. Uranyl powder can be produced, and as a result, uranyl fluoride powder which is easy to handle and has excellent fluidity can be continuously produced. Further, by changing the supply ratio of uranium hexafluoride supplied to the first and second supply nozzles, the average particle size and particle size distribution of the uranyl fluoride powder forming the fluidized bed can be set relatively arbitrarily. The uranyl fluoride powder having a desired particle size can be obtained by extracting the generated uranyl fluoride powder from either the upper extraction pipe or the lower extraction pipe.
【図１】本発明の一実施例のフッ化ウラニル粉末の製造
装置の構成図。FIG. 1 is a configuration diagram of an apparatus for producing uranyl fluoride powder according to one embodiment of the present invention.
１０ 反応塔 １１ 分散板 １２ 流動層 １４ ガス噴出管（ガス噴出部） １６ 下部抜出し管（下部抜出し部） １７ 上部抜出し管（上部抜出し部） １８ 固気分離フィルタ（固気分離部） ２３ オフガスコレクタ ２３ａ 凝縮器 ２３ｂ 凝縮液受槽 ２３ｃ 排出管 ２５ 供給ノズル ２６ 第１供給ノズル ２６ａ 六フッ化ウラン第１供給管 ２６ｂ 第１流量調整弁 ２７ 第２供給ノズル ２７ａ 六フッ化ウラン第２供給管 ２７ｂ 第２流量調整弁 ３０ コントローラ DESCRIPTION OF SYMBOLS 10 Reaction tower 11 Dispersion plate 12 Fluidized bed 14 Gas ejection pipe (gas ejection part) 16 Lower extraction pipe (lower extraction part) 17 Upper extraction pipe (upper extraction part) 18 Solid-gas separation filter (solid-gas separation part) 23 Off-gas collector 23a condenser 23b condensed liquid receiving tank 23c discharge pipe 25 supply nozzle 26 first supply nozzle 26a uranium hexafluoride first supply pipe 26b first flow rate control valve 27 second supply nozzle 27a uranium hexafluoride second supply pipe 27b second Flow control valve 30 Controller
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭46−1767（ＪＰ，Ａ) 特開 昭51−137700（ＪＰ，Ａ) 特開 昭63−134521（ＪＰ，Ａ) 特公 昭37−2003（ＪＰ，Ｂ１) (58)調査した分野(Int.Cl.7，ＤＢ名) C01G 43/06 B01J 8/24 301 ──────────────────────────────────────────────────続 き Continuation of the front page (56) References JP-A-46-1767 (JP, A) JP-A-51-137700 (JP, A) JP-A-63-134521 (JP, A) 2003 (JP, B1) (58) Field surveyed (Int. Cl. 7 , DB name) C01G 43/06 B01J 8/24 301
Claims (2)
を水蒸気により高温で加水分解する流動層(12)と、 前記反応塔(10)内に六フッ化ウランを供給する供給ノズ
ル(25)と、 前記反応塔(10)の底部に設けられ前記水蒸気を前記流動
層(12)に向けて噴出するガス噴出部(14)と、 前記反応塔(10)の上部に設けられ前記加水分解により生
成して上昇するフッ化水素ガスと前記加水分解により生
成し前記ガスに同伴して浮上するフッ化ウラニル粉末と
を分離する固気分離部(18)と、 前記流動層(12)の表面部近傍の前記反応塔(10)に設けら
れ前記表面部で生成されたフッ化ウラニル粉末を抜出す
上部抜出し部(17)と、 前記流動層(12)の深部近傍の前記反応塔(10)に設けられ
前記深部で生成されたフッ化ウラニル粉末を抜出す下部
抜出し部(16)とを備えたフッ化ウラニル粉末の製造装置
において、 前記供給ノズル(25)が前記流動層(12)の表面部に相応す
る位置の前記反応塔(10)に設けられた第１供給ノズル(2
6)と、前記流動層(12)の深部に相応する位置の反応塔(1
0)に設けられた第２供給ノズル(27)とにより構成された
ことを特徴とするフッ化ウラニル粉末の製造装置。1. A fluidized bed (12) formed in a reaction tower (10) for hydrolyzing uranium hexafluoride at high temperature with steam, and a supply nozzle for supplying uranium hexafluoride into the reaction tower (10). (25), a gas jetting part (14) provided at the bottom of the reaction tower (10) and jetting the steam toward the fluidized bed (12), and a gas jetting part (14) provided at the top of the reaction tower (10). A solid-gas separation section (18) for separating hydrogen fluoride gas generated by hydrolysis and rising and uranyl fluoride powder generated by hydrolysis and floating along with the gas, and the fluidized bed (12) An upper extraction portion (17) provided in the reaction tower (10) near the surface portion of the device to extract the uranyl fluoride powder generated at the surface portion, and the reaction tower (17) near the deep portion of the fluidized bed (12). A uranyl fluoride powder provided with a lower extraction part (16) provided in (10) for extracting the uranyl fluoride powder generated in the deep part In the manufacturing apparatus, the first supply nozzle the supply nozzle (25) is provided in the reaction tower at a position corresponding to the surface portion (10) of the fluidized bed (12) (2
6) and the reaction tower (1) at a position corresponding to the depth of the fluidized bed (12).
And a second supply nozzle (27) provided in (0).
化ウラン第１供給管(26a)に設けられた第１流量調整弁
(26b)と、 第２供給ノズル(27)に接続された六フッ化ウラン第２供
給管(27a)に設けられた第２流量調整弁(27b)と、 前記第１流量調整弁(26b)と第２流量調整弁(27b)とを互
いに独立して制御するコントローラ(30)とを備えた請求
項１記載のフッ化ウラニル粉末の製造装置。2. A first flow control valve provided in a first uranium hexafluoride supply pipe (26a) connected to a first supply nozzle (26).
(26b), a second flow control valve (27b) provided in a uranium hexafluoride second supply pipe (27a) connected to a second supply nozzle (27), and the first flow control valve (26b). The apparatus for producing uranyl fluoride powder according to claim 1, further comprising a controller (30) that controls the second flow control valve (27b) and the second flow control valve (27b) independently of each other.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02011093A JP3183314B2 (en) | 1993-02-08 | 1993-02-08 | Production equipment for uranyl fluoride powder |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02011093A JP3183314B2 (en) | 1993-02-08 | 1993-02-08 | Production equipment for uranyl fluoride powder |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06234528A JPH06234528A (en) | 1994-08-23 |
| JP3183314B2 true JP3183314B2 (en) | 2001-07-09 |
Family
ID=12017983
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP02011093A Expired - Fee Related JP3183314B2 (en) | 1993-02-08 | 1993-02-08 | Production equipment for uranyl fluoride powder |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3183314B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112811470A (en) * | 2020-11-20 | 2021-05-18 | 中核北方核燃料元件有限公司 | Method for preparing high-purity uranyl fluoride powder from uranium hexafluoride by dry method |
-
1993
- 1993-02-08 JP JP02011093A patent/JP3183314B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH06234528A (en) | 1994-08-23 |
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