WO2010067677A1 - 三フッ化塩素の除害方法 - Google Patents
三フッ化塩素の除害方法 Download PDFInfo
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- WO2010067677A1 WO2010067677A1 PCT/JP2009/069027 JP2009069027W WO2010067677A1 WO 2010067677 A1 WO2010067677 A1 WO 2010067677A1 JP 2009069027 W JP2009069027 W JP 2009069027W WO 2010067677 A1 WO2010067677 A1 WO 2010067677A1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—Gas phase processes, e.g. by using aerosols
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/108—Halogens or halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/202—Single element halogens
- B01D2257/2027—Fluorine
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
Definitions
- the present invention relates to a method for removing a mixed gas composed of chlorine trifluoride and fluorine.
- chlorine trifluoride (ClF 3 ) is widely known to be synthesized by a direct reaction between chlorine and fluorine (Non-patent Documents 1 and 2).
- ClF 3 produced in the reactor is passed through a cold trap, only the desired product are selectively collected.
- the gas that has passed through the cold collector contains unreacted F 2 gas and ClF 3 that could not be collected. Therefore, the wet scrubber (exhaust gas treatment device) using water or an alkali solution was used. Detoxified.
- ClO 3 F perchloryl fluoride
- ClO 3 F is a thermally stable compound and does not thermally decompose unless heated to 470 ° C. In addition, it is insoluble in water and cannot be decomposed with acid or alkali.
- physical properties are ClO 3 F in the gas similar to ClO 3 F when included at a low concentration, since it is also difficult separation and concentration by distillation, there is removed the problem that difficulty.
- Patent Document 1 As a countermeasure for the above problem, as a method for removing fluorine gas or oxygen fluoride from a fluorine-containing gas, a method using an absorbent containing a sulfur-based reducing agent and a basic compound has been proposed (Patent Document 1).
- the present invention provides a detoxification method capable of suppressing the generation of ClO 3 F which is a hardly decomposable substance when detoxifying a mixed gas containing ClF 3 and F 2 with a wet scrubber.
- the present inventors have provided a heating reaction section in a stage prior to the detoxification treatment of the mixed gas containing ClF 3 and F 2 with a wet scrubber, and the following reaction formula 4 As shown in FIG. 4, by adding halogen gas to the mixed gas, unreacted fluorine gas is reacted with halogen gas, greatly reducing unreacted fluorine gas, and detoxification of ClF 3 using a conventional wet scrubber The inventors have found that it is possible to suppress the generation of ClO 3 F, which is a hardly decomposable substance, which has been a problem in the method, and have reached the present invention.
- the present invention is a method of detoxifying a mixed gas composed of chlorine trifluoride and fluorine with a wet scrubber, and in the pre-stage of the detoxifying process with a wet scrubber, the mixed gas contains a halogen gas X 2.
- a detoxification method characterized in that fluorine is reduced and generation of perchloryl fluoride generated by a wet scrubber is prevented in advance.
- the present invention can significantly reduce unreacted fluorine gas in the pre-stage of the detoxification treatment with the wet scrubber, so that fluoridation such as oxygen difluoride (OF 2 ) which is highly toxic in the wet scrubber. It is also effective in suppressing the generation of oxygen compounds.
- fluoridation such as oxygen difluoride (OF 2 ) which is highly toxic in the wet scrubber. It is also effective in suppressing the generation of oxygen compounds.
- interhalogen gases such as ClF 5 , ClF, BrF 5 , BrF 3 , BrF, IF 7 , IF 5 , IF 3 , IF, NF 3 are included in the mixed gas of chlorine trifluoride and fluorine to be treated. Does not prevent it from being included.
- a halogen gas other than fluorine is used as a raw material gas for reducing unreacted fluorine gas, and chlorine, bromine, or iodine can be used.
- the halogen gas other than fluorine to be added is preferably added in an amount of 1.0 equivalent or more with respect to the unreacted fluorine gas.
- halogen gas other than fluorine to be added can be used without being diluted, but it can also be diluted with an inert gas such as nitrogen or argon.
- the material used for the reactor is preferably nickel or monel, which has high resistance to fluorine gas at high temperatures and has sufficient mechanical strength.
- the reaction temperature is preferably 200 ° C. to 400 ° C., particularly preferably 300 ° C. to 350 ° C.
- the reaction is difficult to proceed at a temperature lower than 200 ° C., and a temperature higher than 400 ° C. is not preferable because the reactor may be significantly corroded.
- the mixed gas introduced into the reactor is preferably retained for at least 30 seconds.
- wet scrubber used for the detoxification treatment it is preferable to use a scrubber using water or an alkaline solution, and it is particularly preferable to use a water scrubber in the first stage and an alkali scrubber in the second stage.
- a KOH solution a NaOH solution, or the like can be used, but it is particularly preferable to use a KOH solution having a relatively high solubility in water.
- FIG. 1 shows a schematic system diagram of an experiment using the present invention.
- the mass flow controllers 1 and 2 individually control the flow rate of the halogen gas, the mixed gas of chlorine trifluoride gas and fluorine gas, and introduce the gas into the nickel tubular reactor 3.
- the nickel cylindrical reactor 3 can be heated to a predetermined temperature by a heater 4 installed outside.
- the water and KOH concentration connected to the subsequent stage of the nickel cylindrical reactor 3 are 0.1 mol / l.
- a detoxification treatment operation is carried out by scrubbers (exhaust gas treatment devices) 5 and 6 of the alkaline solution.
- outlet gas of the scrubber circulation is sampled and analyzed by FT-IR (IG-1000 manufactured by Otsuka Electronics Co., Ltd.) to measure the ClO 3 F concentration.
- Example 1 The outer wall temperature of the nickel cylindrical reactor 3 having an inner diameter of 30 mm and a length of 600 mm was set to 350 ° C., and a mass flow controller 1 was used to mix a mixed gas of 2.8 mol% fluorine gas and 3.5 mol% ClF 3. Using a mass flow controller 2 at 75 ml / min, 3.4 mol% chlorine gas was introduced into the nickel tubular reactor 3 at a flow rate of 10 ml / min, reacted for 30 seconds, and then water connected to the subsequent stage.
- Example 1 The test was performed under the same conditions as in Example 1 except that no chlorine gas was added. As a result, the ClO 3 F concentration in the sampled gas was 6000 volppm.
- Example 2 The outer wall temperature of the nickel cylindrical reactor 3 having an inner diameter of 12.4 mm and a length of 1000 mm is set to 350 ° C., and the mass flow controller 1 is used to mix 5.0 mol% fluorine gas and 3.0 mol% ClF 3 . Using a mass flow controller 2 with a gas flow of 493 ml / min, 6.0 mol% chlorine gas was introduced into the nickel cylindrical reactor 3 at a flow rate of 44 ml / min, reacted for 30 seconds, and then connected to the subsequent stage.
- Example 2 It carried out on the same conditions as Example 2 except not adding chlorine gas. As a result, the ClO 3 F concentration in the sampled gas was 3500 vol ppm.
- Example 3 The outer wall temperature of the nickel cylindrical reactor 3 having an inner diameter of 30 mm and a length of 600 mm was set to 370 ° C., and a mass flow controller 1 was used to mix a mixed gas of 2.8 mol% fluorine gas and 3.5 mol% ClF 3. Using a mass flow controller 2 at 75 ml / min, 3.4 mol% chlorine gas was introduced into the nickel tubular reactor 3 at a flow rate of 10 ml / min, reacted for 30 seconds, and then water connected to the subsequent stage.
- Example 3 It carried out on the same conditions as Example 3 except not adding chlorine gas. As a result, the ClO 3 F concentration in the sampled gas was 5600 volppm.
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Abstract
Description
内径30mm、長さ600mmのニッケル製筒型反応器3の外壁温度を350℃に設定し、マスフローコントローラー1を用いて、2.8mol%のフッ素ガスと3.5mol%のClF3の混合ガスを75ml/min、マスフローコントローラー2を用いて、3.4mol%の塩素ガスを10ml/minの流量で、ニッケル製筒型反応器3に導入し、30秒反応させたあと、後段に連結された水とKOH濃度が0.1mol/lのアルカリ溶液のスクラバー(排ガス処理装置)5、6によって除害処理した後、スクラバー流通の出口ガスをサンプリングし、FT-IR(大塚電子社製 IG-1000)を用いてClO3F濃度を分析したところ、180volppmであった。
塩素ガスを添加しない以外は、実施例1と同条件で行った。その結果、サンプリングしたガス中のClO3F濃度は6000volppmであった。
内径12.4mm、長さ1000mmのニッケル製筒型反応器3の外壁温度を350℃に設定し、マスフローコントローラー1を用いて、5.0mol%のフッ素ガスと3.0mol%のClF3の混合ガスを493ml/min、マスフローコントローラー2を用いて、6.0mol%の塩素ガスを44ml/minの流量で、ニッケル製筒型反応器3に導入し、30秒反応させたあと、後段に連結された水とKOH濃度が0.1mol/lのアルカリ溶液のスクラバー(排ガス処理装置)5、6によって除害処理した後、スクラバー流通の出口ガスをサンプリングし、FT-IR(大塚電子社製 IG-1000)を用いてClO3F濃度を分析したところ、4volppmであった。
塩素ガスを添加しない以外は、実施例2と同条件で行った。その結果、サンプリングしたガス中のClO3F濃度は3500volppmであった。
内径30mm、長さ600mmのニッケル製筒型反応器3の外壁温度を370℃に設定し、マスフローコントローラー1を用いて、2.8mol%のフッ素ガスと3.5mol%のClF3の混合ガスを75ml/min、マスフローコントローラー2を用いて、3.4mol%の塩素ガスを10ml/minの流量で、ニッケル製筒型反応器3に導入し、30秒反応させたあと、後段に連結された水とKOH濃度が0.1mol/lのアルカリ溶液のスクラバー(排ガス処理装置)5、6によって除害処理した後、スクラバー流通の出口ガスをサンプリングし、FT-IR(大塚電子社製 IG-1000)を用いてClO3F濃度を分析したところ、160volppmであった。
塩素ガスを添加しない以外は、実施例3と同条件で行った。その結果、サンプリングしたガス中のClO3F濃度は5600volppmであった。
Claims (3)
- 少なくとも三フッ化塩素及びフッ素から成る混合ガスを、湿式スクラバーによって除害処理する方法であって、
湿式スクラバーによる除害処理の前段階において、前記混合ガスに、ハロゲンガスX2(X=Cl、Br又はIを示す。)を添加し、前記混合ガス中のフッ素とハロゲンガスX2(X=Cl、Br又はIを示す。)を反応させることによって、前記混合ガス中のフッ素を低減し、湿式スクラバーで生成するフッ化ペルクロリル(ClO3F)の生成を未然に防止することを特徴とする除害方法。 - 前記混合ガス中のフッ素ガスに対し1.0当量以上のハロゲンガスX2(X=Cl又はBr又はIを示す。)を添加することを特徴とする請求項1に記載の方法。
- 前記混合ガス中のフッ素とハロゲンガスX2(X=Cl、Br又はIを示す。)を200℃~400℃の温度範囲で反応させることを特徴とする請求項1又は請求項2に記載の方法。
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CN2009801344047A CN102143793B (zh) | 2008-12-11 | 2009-11-09 | 三氟化氯的除害方法 |
KR1020117008395A KR101343961B1 (ko) | 2008-12-11 | 2009-11-09 | 3불화염소 및 불소를 포함하는 혼합 가스의 제해 방법 |
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CN104477849B (zh) * | 2014-12-02 | 2016-08-17 | 中国船舶重工集团公司第七一八研究所 | 一种三氟化氯的制备方法 |
CN104555927B (zh) * | 2014-12-31 | 2016-07-20 | 中国船舶重工集团公司第七一八研究所 | 一种三氟化氯的纯化方法 |
JP6895623B2 (ja) * | 2017-02-21 | 2021-06-30 | セントラル硝子株式会社 | ヨウ素化合物の除去方法 |
Citations (3)
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JPH11128676A (ja) * | 1997-10-31 | 1999-05-18 | Japan Pionics Co Ltd | 有害ガスの浄化方法 |
JP2000093745A (ja) * | 1998-09-22 | 2000-04-04 | Kashiyama Kogyo Kk | 排ガス処理方法および処理装置 |
JP2004351364A (ja) * | 2003-05-30 | 2004-12-16 | Ebara Corp | 三フッ化塩素を含む無機ハロゲン化ガス含有排ガスの処理方法、処理剤及び処理装置 |
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US5935540A (en) * | 1997-04-25 | 1999-08-10 | Japan Pionics Co., Ltd. | Cleaning process for harmful gas |
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- 2009-11-09 WO PCT/JP2009/069027 patent/WO2010067677A1/ja active Application Filing
- 2009-11-09 CN CN2009801344047A patent/CN102143793B/zh active Active
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JPH11128676A (ja) * | 1997-10-31 | 1999-05-18 | Japan Pionics Co Ltd | 有害ガスの浄化方法 |
JP2000093745A (ja) * | 1998-09-22 | 2000-04-04 | Kashiyama Kogyo Kk | 排ガス処理方法および処理装置 |
JP2004351364A (ja) * | 2003-05-30 | 2004-12-16 | Ebara Corp | 三フッ化塩素を含む無機ハロゲン化ガス含有排ガスの処理方法、処理剤及び処理装置 |
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CN102143793A (zh) | 2011-08-03 |
JP5471313B2 (ja) | 2014-04-16 |
KR20110069069A (ko) | 2011-06-22 |
CN102143793B (zh) | 2013-12-18 |
JP2010158664A (ja) | 2010-07-22 |
KR101343961B1 (ko) | 2013-12-20 |
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