JPH07300302A - Production of chlorine dioxide - Google Patents
Production of chlorine dioxideInfo
- Publication number
- JPH07300302A JPH07300302A JP12047494A JP12047494A JPH07300302A JP H07300302 A JPH07300302 A JP H07300302A JP 12047494 A JP12047494 A JP 12047494A JP 12047494 A JP12047494 A JP 12047494A JP H07300302 A JPH07300302 A JP H07300302A
- Authority
- JP
- Japan
- Prior art keywords
- tower
- chlorine dioxide
- aqueous solution
- reaction
- air
- 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.)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
【0001】[0001]
【産業上の利用分野】本発明は、二酸化塩素の製造法に
関し、更に詳しくは、安価且つ簡単な装置を用い、純度
の高い二酸化塩素を容易に製造することのできる二酸化
塩素の製造法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for producing chlorine dioxide, and more particularly to a method for producing chlorine dioxide which can be easily produced with high purity using inexpensive and simple equipment.
【0002】二酸化塩素は酸化力が強く優れた殺菌能力
を有するため、製紙用木材パルプの漂白、工業用水や飲
料水、下水道の消毒、魚介類や野菜、果物等、更には家
畜舎の消毒、臭気抑制剤として使用されている。Since chlorine dioxide has a strong oxidizing power and an excellent sterilizing ability, it bleaches wood pulp for papermaking, disinfects industrial water and drinking water, sewerage, disinfects seafood, vegetables, fruits and the like, and further disinfects livestock houses, Used as an odor control agent.
【0003】[0003]
【従来の技術】従来、二酸化塩素の製造方法としては、
例えば特開平4−342402号には、ベンチュリ管を
備えた反応室に塩素酸塩の水溶液と酸のガス流を導入し
て反応させて二酸化塩素を生成させ、更に推進媒体を導
入して二酸化塩素と混合する方法が開示されている。2. Description of the Related Art Conventionally, as a method for producing chlorine dioxide,
For example, in Japanese Unexamined Patent Publication (Kokai) No. 4-342402, an aqueous solution of chlorate and a gas flow of an acid are introduced into a reaction chamber equipped with a Venturi tube to react with each other to generate chlorine dioxide, and a propulsion medium is introduced to introduce chlorine dioxide. A method of mixing with is disclosed.
【0004】[0004]
【発明が解決しようとする課題】しかし乍ら、上記方法
は、ベンチュリ管を使用し瞬間時に反応させるため、原
料や媒体の流量等の反応条件の調整及び設定が極めて難
しく、等量での完全な混合及び反応は至難又は殆ど不可
能に近い。その結果、反応効率が悪くなって未反応原料
が製品中に混入し、製品の純度を低下せしめるに至る。
また、二酸化塩素は同時に生成する塩素との混合物とし
て得られるため、二酸化塩素の純度が低く、それだけ二
酸化塩素の優れた酸化力や殺菌能力が減じられ、用途に
よっては使用が制限されるという問題がある。この問題
を解決するには、二酸化塩素と塩素とを分離する装置が
必要不可欠となり、装置コストが上昇するという憾みが
ある。本発明は上記問題を解決し、安価且つ簡単な装置
により、高純度の二酸化塩素を容易に製造することので
きる方法を提供するものである。However, in the above method, the reaction conditions such as the flow rate of the raw material and the medium are extremely difficult to adjust and set because the Venturi tube is used for the reaction at the moment, so that the same amount is used. Mixing and reaction is difficult or nearly impossible. As a result, the reaction efficiency becomes poor and unreacted raw materials are mixed in the product, resulting in a decrease in the purity of the product.
Also, since chlorine dioxide is obtained as a mixture with chlorine that is produced at the same time, the purity of chlorine dioxide is low, the excellent oxidizing power and sterilizing ability of chlorine dioxide are reduced, and the use is limited depending on the application. is there. In order to solve this problem, an apparatus for separating chlorine dioxide and chlorine becomes indispensable, and the apparatus cost is increased. The present invention solves the above problems and provides a method capable of easily producing high-purity chlorine dioxide with an inexpensive and simple apparatus.
【0005】[0005]
【課題を解決するための手段】即ち、本発明の第1は、
循環塔を上部及び下部で連通するように接続した反応塔
の下部から塩素酸塩水溶液、酸のガス及び不活性ガスを
導入し、エアリフトにより反応塔内及び循環塔内を循環
させ乍ら反応させ、生成した二酸化塩素を塩素ガスとと
もに反応塔の上部より取り出すことを特徴とする二酸化
塩素の製造法を、That is, the first aspect of the present invention is to:
A chlorate aqueous solution, an acid gas and an inert gas are introduced from the lower part of the reaction tower, which is connected so that the circulation tower is in communication with the upper part and the lower part, and is circulated in the reaction tower and the circulation tower by an air lift to cause a reaction. The chlorine dioxide production method is characterized in that the produced chlorine dioxide is taken out from the upper part of the reaction tower together with chlorine gas.
【0006】本発明の第2は、上記第1の発明におい
て、生成した二酸化塩素を水溶液とともに取り出し、該
二酸化塩素と水溶液を脱気塔に導き、塔底部より不活性
ガスを導入して脱気を行い、塔頂部より二酸化塩素を不
活性ガスとともに回収するとともに、水溶液を反応塔に
戻す製造法を、In a second aspect of the present invention, the chlorine dioxide produced in the first aspect is taken out together with the aqueous solution, the chlorine dioxide and the aqueous solution are introduced into a degassing tower, and an inert gas is introduced from the bottom of the tower to degas. And recover chlorine dioxide from the top of the tower together with the inert gas and return the aqueous solution to the reaction tower.
【0007】本発明の第3は、循環塔を上部及び下部で
連通するように接続した反応塔の下部から亜塩素酸塩水
溶液、塩素ガス及び不活性ガスを導入し、エアリフトに
より反応塔内及び循環塔内を循環させ乍ら反応させ、生
成した二酸化塩素を反応塔の上部より取り出すことを特
徴とする二酸化塩素の製造法を、A third aspect of the present invention is to introduce an aqueous chlorite solution, chlorine gas and an inert gas from the lower part of the reaction tower, which is connected so that the circulation tower communicates with the upper part and the lower part, and to introduce the chlorite solution into the reaction tower by air lift. A method for producing chlorine dioxide characterized in that the chlorine dioxide produced is taken out from the upper part of the reaction tower by circulating the reaction in the circulation tower and reacting it.
【0008】本発明の第4は、上記第3の発明におい
て、生成した二酸化塩素を水溶液とともに取り出し、該
二酸化塩素と水溶液を脱気塔に導き、塔底部より不活性
ガスを導入して脱気を行い、塔頂部より二酸化塩素を不
活性ガスとともに回収するとともに、水溶液を反応塔に
戻す請求項1記載の製造法を、それぞれ内容とするもの
である。In a fourth aspect of the present invention, the chlorine dioxide produced in the third aspect is taken out together with the aqueous solution, the chlorine dioxide and the aqueous solution are introduced into a degassing tower, and an inert gas is introduced from the bottom of the tower to degas. And recovering chlorine dioxide together with an inert gas from the top of the tower, and returning the aqueous solution to the reaction tower.
【0009】本発明に用いられる装置の一例を図面に基
づいて説明する。図1において、反応装置は反応塔1と
循環塔2とからなり、両塔は上部及び下部で互いに連通
した構造からなる。反応塔1の下部には第1原料導入ラ
イン3、第2原料導入ライン4、及び不活性ガスの導入
ライン5がそれぞれ設けられ、これらは反応塔1の下部
の導入口6に連絡している。7は多孔板である。An example of an apparatus used in the present invention will be described with reference to the drawings. In FIG. 1, the reactor comprises a reaction tower 1 and a circulation tower 2, and both towers have a structure in which an upper part and a lower part communicate with each other. A first raw material introduction line 3, a second raw material introduction line 4, and an inert gas introduction line 5 are provided in the lower part of the reaction tower 1, and these are connected to an introduction port 6 in the lower part of the reaction tower 1. . 7 is a perforated plate.
【0010】反応塔1の上部には取出口8が設けられ、
更に塔頂部には排出ライン9が設けられている。一方、
循環塔2内には、熱交換器10が設けられている。An outlet 8 is provided at the top of the reaction tower 1,
Further, a discharge line 9 is provided at the top of the tower. on the other hand,
A heat exchanger 10 is provided in the circulation tower 2.
【0011】図2は本発明に用いられる他の装置を示
し、図1で示した装置に、更に脱気塔12が設けられて
いる。脱気塔12は下部には不活性ガスの導入口13
を、上部には不活性ガスと生成物(二酸化塩素)の排出
口14を備え、更に脱気塔12は上方において反応塔1
の取出口8と移送ライン15を介して接続されるととも
に、下方において循環塔2と戻しライン16を介して接
続されている。FIG. 2 shows another apparatus used in the present invention. The apparatus shown in FIG. 1 is further provided with a degassing tower 12. The degassing tower 12 has an inert gas inlet 13 at the bottom.
And an outlet 14 for the inert gas and the product (chlorine dioxide) is provided at the upper part, and the degassing tower 12 is located above the reaction tower 1
Is connected via the transfer line 15 and the circulation tower 2 below via the return line 16.
【0012】以下、上記装置を用いて本発明を実施する
方法について説明する。尚、反応媒体として水、酸のガ
スとして塩化水素ガス、不活性ガスとして空気を例に挙
げて説明する。反応塔1及び循環塔2内に予め水を充填
しておき、第1原料導入ライン3から塩素酸塩水溶液
を、第2原料導入ライン4から塩化水素ガスを、不活性
ガス導入ライン5からの空気とともに導入口6より反応
塔1の下部に導入する。A method for carrying out the present invention using the above apparatus will be described below. In the following description, water is used as a reaction medium, hydrogen chloride gas is used as an acid gas, and air is used as an inert gas. Water is previously filled in the reaction tower 1 and the circulation tower 2, and an aqueous chlorate solution is supplied from the first raw material introduction line 3, hydrogen chloride gas is supplied from the second raw material introduction line 4, and an inert gas introduction line 5 is supplied. It is introduced into the lower part of the reaction tower 1 through the inlet 6 together with air.
【0013】導入された塩素酸塩水溶液、塩化水素ガス
及び空気は多孔板7を通過し、このとき空気は細かな気
泡となり、そのエアリフト作用により塩素酸塩水溶液及
び塩化水素ガスとともに反応塔1内を上昇し、循環塔2
内に導かれる。循環塔2内に導かれた塩素酸塩水溶液、
塩化水素ガス及び空気は熱交換器10により冷却され比
重が大きくなって下降して反応塔1内に入り、再びエア
リフト作用により上昇し、反応塔1内と循環塔2内の循
環を繰り返す。The introduced chlorate aqueous solution, hydrogen chloride gas and air pass through the perforated plate 7, and at this time, the air becomes fine bubbles, and the air lift action causes the air inside the reaction tower 1 together with the chlorate aqueous solution and hydrogen chloride gas. Ascend and circulation tower 2
Be guided inside. Chlorate aqueous solution introduced into the circulation tower 2,
The hydrogen chloride gas and the air are cooled by the heat exchanger 10, have a large specific gravity, descend and descend into the reaction tower 1 and rise again by the air lift action, and the circulation in the reaction tower 1 and the circulation tower 2 is repeated.
【0014】上記循環を繰り返し乍ら塩素酸塩水溶液と
塩化水素ガスは反応して二酸化塩素を生成し、副生した
塩素ガスとともに反応塔頂部の排出ライン9より混合物
として排出回収される。一方、副生した食塩を含む水溶
液は取出口8よりオーバーフローさせ取り出される。By repeating the above circulation, the aqueous chlorate solution and hydrogen chloride gas react with each other to produce chlorine dioxide, which is discharged and recovered as a mixture from the discharge line 9 at the top of the reaction column together with chlorine gas produced as a by-product. On the other hand, the by-produced aqueous solution containing salt overflows from the outlet 8 and is taken out.
【0015】次に、図2に示す装置を用いる場合につい
て説明する。原料及び空気の導入、並びに反応について
は上記と同様に行われる。副生した塩素ガスは反応塔頂
部の排出ライン9より排出され、アルカリ処理により次
亜塩素酸ナトリウムの製造等に利用される。一方、生成
した二酸化塩素は、副生した食塩を含む水溶液とともに
取出口8より取り出され、移送ライン15を経由して脱
気塔12内に導入され、下部の導入口13から導入され
た空気と接触せしめられ、二酸化塩素は上部の排出口1
4から空気とともに回収され、一方、二酸化塩素と分離
された水溶液は未反応原料を少量を含むので戻しライン
16を経由して循環塔2内に戻され、再び反応に供され
る。以上から明らかなように、図2の装置を用いる場合
は、特別な分離装置を用いることなく、副生した塩素ガ
スを含まない高純度の二酸化塩素を得ることができる。Next, the case of using the apparatus shown in FIG. 2 will be described. The introduction of raw materials and air, and the reaction are carried out in the same manner as above. The chlorine gas produced as a by-product is discharged from the discharge line 9 at the top of the reaction tower, and is used for the production of sodium hypochlorite by the alkali treatment. On the other hand, the produced chlorine dioxide is taken out from the outlet 8 together with the aqueous solution containing by-produced salt, introduced into the deaeration tower 12 via the transfer line 15, and the air introduced from the lower inlet 13. Chlorine dioxide is brought into contact and chlorine dioxide is discharged from the upper outlet 1
On the other hand, the aqueous solution which has been recovered together with air from 4, and which has been separated from chlorine dioxide, contains a small amount of unreacted raw material, and therefore is returned to the circulation tower 2 via the return line 16 and is again used for the reaction. As is apparent from the above, when the apparatus of FIG. 2 is used, high-purity chlorine dioxide containing no chlorine gas produced as a by-product can be obtained without using a special separation apparatus.
【0016】第1原料として亜塩素酸水溶液を用い、第
2原料として塩素ガスを用いる場合も、上記と同様の操
作でよいが、この場合は副生物としての塩素は生成しな
い。従って、排出ライン9から二酸化塩素を回収し、食
塩水溶液を取出口8からオーバーフローさせて取り出す
ことができ、高純度の二酸化塩素を得ることが可能であ
る。また亜塩素酸水溶液は塩素酸塩水溶液と併用するこ
とも可能である。この場合は、上記した塩素酸塩水溶液
と塩化水素とを反応させ二酸化塩素を生成させる過程に
おいて、導入口11より亜塩素酸水溶液を反応塔内に導
入し、塩素酸塩水溶液と塩化水素ガスとの反応で副生す
る塩素ガスと反応させ二酸化塩素を生成させることがで
きる。When an aqueous chlorous acid solution is used as the first raw material and chlorine gas is used as the second raw material, the same operation as described above may be performed, but in this case, chlorine as a by-product is not produced. Therefore, chlorine dioxide can be recovered from the discharge line 9, the saline solution can be overflowed from the outlet 8 and taken out, and high-purity chlorine dioxide can be obtained. The chlorous acid aqueous solution can be used in combination with the chlorate aqueous solution. In this case, in the process of reacting the aqueous chlorate solution with hydrogen chloride to generate chlorine dioxide, the aqueous chlorous acid solution is introduced into the reaction tower through the inlet 11 to generate an aqueous chlorate solution and hydrogen chloride gas. It is possible to generate chlorine dioxide by reacting with chlorine gas which is a by-product of the reaction.
【0017】本発明において用いられる塩素酸塩水溶液
の濃度は10〜40重量%が好ましく、また亜塩素酸水
溶液の濃度は5〜25重量%が好ましい。酸のガスとし
てはハロゲン酸が好ましく、特に塩化水素ガスが好適で
ある。不活性ガスとしては、窒素、空気等が好ましい
が、特に空気が好適である。また反応媒体としては水が
好ましく、更に反応温度は0〜40℃の範囲が好まし
い。The concentration of the aqueous chlorate solution used in the present invention is preferably 10 to 40% by weight, and the concentration of the aqueous chlorite solution is preferably 5 to 25% by weight. As the acid gas, halogen acid is preferable, and hydrogen chloride gas is particularly preferable. Nitrogen, air and the like are preferable as the inert gas, but air is particularly preferable. Water is preferable as the reaction medium, and the reaction temperature is preferably in the range of 0 to 40 ° C.
【0018】[0018]
【実施例】以下、実施例に基づいて本発明を更に詳しく
説明するが、本発明はこれらのみに限定されるものでは
ない。The present invention will be described in more detail based on the following examples, but the invention is not intended to be limited thereto.
【0019】実施例1 図1に示した装置(反応塔容積23L)を使用した。反
応塔内に予め水を充填し、40重量%塩素酸ナトリウム
水溶液を73g/分、無水塩化水素ガスを11L/分、
空気を47L/分の速度でそれぞれ反応塔下部より供給
した。エアーリフトによる液循環を確認し、反応ゾーン
温度を25℃に維持し安定状態になった時点で、試料分
析を実施した。副生する食塩を含む食塩水溶液は60g
/分でオーバーフローさせた。目的とする二酸化塩素
は、副生した塩素ガスと空気が混在する混合物として回
収された。回収された二酸化塩素混合物を、ANSI/
AWWA標準法B303−88に準拠して分析したとこ
ろ、二酸化塩素生成量は14.3g/分(0.21 mol
/分)、塩素生成量は7.4g/分(0.10 mol/
分)であった。これは原料塩素酸ナトリウム供給量に対
し二酸化塩素の収率は78%、塩素の収率は76%にな
る。無水塩化水素ガス供給量に対し、二酸化塩素の収率
は86%、塩素の収率は84%に相当するものであっ
た。Example 1 The apparatus (reaction tower volume 23 L) shown in FIG. 1 was used. Water was charged in advance in the reaction tower, a 40 wt% sodium chlorate aqueous solution was 73 g / min, and anhydrous hydrogen chloride gas was 11 L / min.
Air was supplied from the lower part of the reaction tower at a rate of 47 L / min. When the liquid circulation by the air lift was confirmed and the reaction zone temperature was maintained at 25 ° C. and a stable state was reached, sample analysis was performed. 60g of salt solution containing salt as a by-product
Overflow at / min. The target chlorine dioxide was recovered as a mixture of chlorine gas by-produced and air. The recovered chlorine dioxide mixture is treated with ANSI /
When analyzed according to AWWA Standard Method B303-88, the chlorine dioxide production was 14.3 g / min (0.21 mol
/ Min), the amount of chlorine produced is 7.4 g / min (0.10 mol / min)
Minutes). This means that the yield of chlorine dioxide is 78% and the yield of chlorine is 76% with respect to the amount of raw material sodium chlorate supplied. The chlorine dioxide yield was 86% and the chlorine yield was 84% with respect to the amount of anhydrous hydrogen chloride gas supplied.
【0020】実施例2 図2に示した脱気塔を備えた装置を用い、同様の実験を
実施した。40重量%塩素酸ナトリウム水溶液を73g
/分、無水塩化水素ガスを11L/分、空気を47L/
分の速度でそれぞれ反応塔下部より供給した。反応ゾー
ン温度を6℃に、脱気塔温度を20℃にそれぞれ維持し
た。二酸化塩素を含む食塩水溶液を1L/分でオーバー
フローさせて取り出し、これを脱気塔に導き、脱気塔の
塔頂部に導入した。空気を47L/分の速度で塔底部よ
り供給し、脱気を行って二酸化塩素を分離し、残った水
溶液を循環塔の熱交換器の手前に再度供給循環した。エ
アーリフトによる液循環を安定状態に維持して試料分析
を実施した。副生する塩素ガスは反応塔の塔頂部より排
出され、アルカリ処理により次亜鉛素酸ナトリウム等の
製造に利用される。脱気塔の塔頂部より目的とする二酸
化塩素は空気と共に回収された。実施例1と同様にAN
SI/AWWA標準法B303−88に準拠して分析し
たところ、二酸化塩素生成量は12.5g/分(0.1
8 mol/分)であった。混在する副生塩素ガスは0.8
g/分(0.01 mol/分)であった。二酸化塩素の収
率は、原料塩素酸ナトリウム供給量に対し68%、無水
塩化水素ガス供給量に対し76%にそれぞれ相当するも
のであった。Example 2 A similar experiment was carried out using the apparatus equipped with the degassing tower shown in FIG. 73 g of 40 wt% sodium chlorate aqueous solution
/ Min, anhydrous hydrogen chloride gas 11 L / min, air 47 L / min
Each was supplied from the lower part of the reaction tower at a rate of minutes. The reaction zone temperature was maintained at 6 ° C and the degassing tower temperature was maintained at 20 ° C. The saline solution containing chlorine dioxide was taken out by overflowing at 1 L / min, introduced into a degassing tower, and introduced at the top of the degassing tower. Air was supplied from the bottom of the tower at a rate of 47 L / min, deaeration was performed to separate chlorine dioxide, and the remaining aqueous solution was again supplied and circulated before the heat exchanger of the circulation tower. The sample analysis was performed while maintaining the liquid circulation by the air lift in a stable state. Chlorine gas produced as a by-product is discharged from the top of the reaction tower and is used for the production of sodium hypozincate, etc. by alkali treatment. The target chlorine dioxide was recovered together with air from the top of the degassing tower. AN as in Example 1
When analyzed in accordance with SI / AWA standard method B303-88, the chlorine dioxide production was 12.5 g / min (0.1
8 mol / min). Mixed by-product chlorine gas is 0.8
It was g / min (0.01 mol / min). The yield of chlorine dioxide was 68% with respect to the supply amount of raw material sodium chlorate, and 76% with respect to the supply amount of anhydrous hydrogen chloride gas.
【0021】実施例3 実施例1と同様にして、25重量%の亜塩素酸ナトリウ
ム水溶液を89g/分、塩素ガスを2.7L/分、空気
を47L/分の速度でそれぞれ反応塔下部より供給し
た。反応ゾーン温度を25℃に維持し安定状態になし、
エアーリフトによる液循環を確認して、試料分析を実施
した。食塩水部分は80g/分でオーバーフローさせ、
目的とする二酸化塩素は空気と混合物として回収され
た。実施例1と同様にANSI/AWWA標準法B30
3−88に準拠して分析したところ、二酸化塩素生成量
は13.0g/分(0.19 mol/分)であった。二酸
化塩素の収率は、原料亜塩素酸ナトリウム供給量に対し
78%に相当するものであった。Example 3 In the same manner as in Example 1, a 25 wt% aqueous sodium chlorite solution was fed from the bottom of the reaction column at a rate of 89 g / min, chlorine gas at 2.7 L / min, and air at a rate of 47 L / min. Supplied. Keeping the reaction zone temperature at 25 ° C and making it stable,
The liquid analysis by the air lift was confirmed, and the sample analysis was performed. The salt solution overflows at 80 g / min,
The desired chlorine dioxide was recovered as a mixture with air. ANSI / AWWA Standard Method B30 as in Example 1
When analyzed in accordance with 3-88, the amount of chlorine dioxide produced was 13.0 g / min (0.19 mol / min). The yield of chlorine dioxide was 78% with respect to the amount of the raw material sodium chlorite supplied.
【0022】実施例4 図1に示した装置を用い、反応塔に予め水を充填し、4
0重量%の塩素酸ナトリウム水溶液を73g/分、無水
塩化水素ガスを11L/分、空気を47L/分の速度で
それぞれ供給するとともに、更に25重量%の亜塩素酸
ナトリウム水溶液を64g/分の速度で供給した。反応
ゾーン温度を25℃に維持し安定状態になし、エアーリ
フトによる液循環を確認して、試料分析を実施した。食
塩水部分は120g/分でオーバーフローさせ、目的と
する二酸化塩素は空気との混合物として回収された。実
施例1と同様にANSI/AWWA標準法B303−8
8に準拠して分析したところ、二酸化塩素生成量は2
6.1g/分(0.38 mol/分)、塩素生成量は1.
6g/分(0.02 mol/分)であった。二酸化塩素の
収率は、原料塩素酸ナトリウムと亜塩素酸ナトリウムと
の合計供給量に対し86%に相当するものであった。Example 4 Using the apparatus shown in FIG.
73 g / min of 0 wt% sodium chlorate aqueous solution, 11 L / min of anhydrous hydrogen chloride gas and 47 L / min of air were supplied respectively, and further 25 wt% sodium chlorite aqueous solution was 64 g / min. Feed at rate. The reaction zone temperature was maintained at 25 ° C., a stable state was achieved, liquid circulation by an air lift was confirmed, and sample analysis was performed. The saline portion overflowed at 120 g / min and the desired chlorine dioxide was recovered as a mixture with air. ANSI / AWWA Standard Method B303-8 as in Example 1
When analyzed according to 8, the amount of chlorine dioxide produced is 2
6.1 g / min (0.38 mol / min), chlorine production was 1.
It was 6 g / min (0.02 mol / min). The yield of chlorine dioxide was equivalent to 86% with respect to the total feed amount of the raw material sodium chlorate and sodium chlorite.
【0023】[0023]
【発明の効果】叙上のとおり、本発明によれば、高純度
の二酸化塩素を安価且つ簡単な装置を用いて容易に製造
することができる。As described above, according to the present invention, high-purity chlorine dioxide can be easily produced using an inexpensive and simple apparatus.
【図1】本発明に用いられる装置の一例を示す概略図で
ある。FIG. 1 is a schematic view showing an example of an apparatus used in the present invention.
【図2】本発明に用いられる装置の他の例を示す概略図
である。FIG. 2 is a schematic view showing another example of the apparatus used in the present invention.
1 反応塔 2 循環塔 3 第1原料導入ライン 4 第2原料導入
ライン 5 不活性ガス導入ライン 6 導入口 7 多孔板 8 取出口 9 排出ライン 10 熱交換器 11 導入口 12 脱気塔 13 導入口 14 排出口 15 移送ライン 16 戻しライン1 Reaction Tower 2 Circulation Tower 3 First Raw Material Introduction Line 4 Second Raw Material Introduction Line 5 Inert Gas Introduction Line 6 Introduction Port 7 Perforated Plate 8 Outlet 9 Exhaust Line 10 Heat Exchanger 11 Inlet 12 Degassing Tower 13 Inlet 14 discharge port 15 transfer line 16 return line
Claims (8)
接続した反応塔の下部から塩素酸塩水溶液、酸のガス及
び不活性ガスを導入し、エアリフトにより反応塔内及び
循環塔内を循環させ乍ら反応させ、生成した二酸化塩素
を塩素ガスとともに反応塔の上部より取り出すことを特
徴とする二酸化塩素の製造法。1. A chlorate aqueous solution, an acid gas and an inert gas are introduced from the lower part of a reaction tower which is connected so that the upper and lower parts of the circulation tower communicate with each other, and is circulated in the reaction tower and the circulation tower by an air lift. A method for producing chlorine dioxide, characterized in that the chlorine dioxide produced is reacted with the chlorine gas and taken out from the upper part of the reaction tower together with chlorine gas.
り出し、該二酸化塩素と水溶液を脱気塔に導き、塔底部
より不活性ガスを導入して脱気を行い、塔頂部より二酸
化塩素を不活性ガスとともに回収するとともに、水溶液
を反応塔に戻す請求項1記載の製造法。2. The chlorine dioxide produced is taken out together with the aqueous solution, the chlorine dioxide and the aqueous solution are introduced into a degassing tower, an inert gas is introduced from the bottom of the tower for degassing, and the chlorine dioxide is inert gas from the top of the tower. The method according to claim 1, wherein the aqueous solution is recovered together with the aqueous solution and returned to the reaction tower.
求項1又は2記載の製造法。3. The production method according to claim 1, wherein an aqueous chlorite solution is introduced into the reaction tower.
接続した反応塔の下部から亜塩素酸塩水溶液、塩素ガス
及び不活性ガスを導入し、エアリフトにより反応塔内及
び循環塔内を循環させ乍ら反応させ、生成した二酸化塩
素を反応塔の上部より取り出すことを特徴とする二酸化
塩素の製造法。4. A chlorite aqueous solution, chlorine gas and an inert gas are introduced from the lower part of the reaction tower which is connected so that the upper and lower parts of the circulation tower communicate with each other, and circulated in the reaction tower and the circulation tower by an air lift. A method for producing chlorine dioxide, characterized in that the chlorine dioxide formed is reacted and then taken out from the upper part of the reaction tower.
り出し、該二酸化塩素と水溶液を脱気塔に導き、塔底部
より不活性ガスを導入して脱気を行い、塔頂部より二酸
化塩素を不活性ガスとともに回収するとともに、水溶液
を反応塔に戻す請求項4記載の製造法。5. The produced chlorine dioxide is taken out together with the aqueous solution, the chlorine dioxide and the aqueous solution are introduced into a degassing tower, an inert gas is introduced from the bottom of the tower for degassing, and the chlorine dioxide is inert gas from the top of the tower. The method according to claim 4, wherein the aqueous solution is recovered together with the aqueous solution and returned to the reaction tower.
項1記載の製造法。6. The method according to claim 1, wherein the acid gas is a halogen acid gas.
請求項6記載の製造法。7. The method according to claim 6, wherein the halogen acid gas is hydrogen chloride gas.
は4記載の製造法。8. The method according to claim 1, wherein the reaction temperature is 0 to 40 ° C.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP12047494A JPH07300302A (en) | 1994-05-09 | 1994-05-09 | Production of chlorine dioxide |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP12047494A JPH07300302A (en) | 1994-05-09 | 1994-05-09 | Production of chlorine dioxide |
Publications (1)
Publication Number | Publication Date |
---|---|
JPH07300302A true JPH07300302A (en) | 1995-11-14 |
Family
ID=14787077
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP12047494A Withdrawn JPH07300302A (en) | 1994-05-09 | 1994-05-09 | Production of chlorine dioxide |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPH07300302A (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100884330B1 (en) * | 2008-08-14 | 2009-02-18 | 이승채 | Apparatus and method for the production of pure aqueous chlorine dioxide solution |
KR100902846B1 (en) * | 2008-05-26 | 2009-06-16 | 이승채 | Apparaus for the production of the pure organic chlrorine dioxide solution and the production method using thereof |
KR100937065B1 (en) * | 2003-08-04 | 2010-01-15 | 다이꼬 야꾸힝 가부시끼가이샤 | Equipment for producing chlorine dioxide |
CN106315513A (en) * | 2016-10-26 | 2017-01-11 | 吴予奇 | Chlorine dioxide gas synthesizer |
KR101696649B1 (en) * | 2016-03-07 | 2017-01-16 | 이동근 | Apparatus for generrating pure chlorine dioxide and method |
-
1994
- 1994-05-09 JP JP12047494A patent/JPH07300302A/en not_active Withdrawn
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100937065B1 (en) * | 2003-08-04 | 2010-01-15 | 다이꼬 야꾸힝 가부시끼가이샤 | Equipment for producing chlorine dioxide |
KR100902846B1 (en) * | 2008-05-26 | 2009-06-16 | 이승채 | Apparaus for the production of the pure organic chlrorine dioxide solution and the production method using thereof |
KR100884330B1 (en) * | 2008-08-14 | 2009-02-18 | 이승채 | Apparatus and method for the production of pure aqueous chlorine dioxide solution |
KR101696649B1 (en) * | 2016-03-07 | 2017-01-16 | 이동근 | Apparatus for generrating pure chlorine dioxide and method |
CN106315513A (en) * | 2016-10-26 | 2017-01-11 | 吴予奇 | Chlorine dioxide gas synthesizer |
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Legal Events
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