JP2010533114A - 気相酸化による塩素の製造方法 - Google Patents
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Abstract
【選択図】 図1
Description
4HCl+O2→2Cl2+2H2O
これらの特許によれば、管束反応器中で固定床法として等温的に進行し、複雑な方法での制御を要する冷却系を必要とする。原理的に、記述されているすべての管束反応器はまた極めて複雑であり、高資本コストを要する。建設サイズと共に急速に上昇する、触媒床の機械的安定性および均一な定温化に関する問題によって、このようなタイプの大型ユニットは不経済なものとなる。
な充填物の形のばらけた、担持触媒または非担持触媒を含んでなる。
ることにより、反応器の構造物の中に導入される触媒の容積と熱交換面積が達成可能である。構造化された触媒の使用の更なる利点は、薄い触媒層中では反応物質の短い拡散経路が必要とされ、触媒選択性の増大と連携可能であるということである。
特に好ましい化合物は、この明細書中では塩化銅(I)、塩化銅(II)、酸化銅(I)、酸化銅(II)、塩化カリウム、塩化ナトリウム、酸化クロム(III)、酸化クロム(IV)、酸化クロム(VI)、酸化ビスマス、酸化ルテニウム、塩化ルテニウム、オキシ塩化ルテニウム、酸化ロジウム、酸化ウラニウム、塩化ウラニウムおよび/またはオキシ塩化ウラニウムを含んでなる。
−触媒床の寸法決定、
−触媒床の間の熱除去の制御、
−触媒床の間のフィードガスの添加、
−反応物質のモル比、
−反応物質の濃度、
−触媒床の上流および/または間での不活性ガス、特に窒素、二酸化炭素の添加。
媒床で上昇させて、触媒活性を増大させ、次に下流の最終触媒床で平均温度を再度下降させて、平衡をシフトさせることが特に有利であり得る。他方、直列に接続されている反応域を上昇する平均温度において運転することが有利であり得る。このように、初期に所望の温度上限からの安全マージンを大きくとって反応物質の転換を行うことができる。低レベルの反応物質が存在する反応後期に平均温度を上昇することにより、転化率を更に進めることができる。
ロセスガス混合物の入口温度は、段階の数の増加と共に上昇する。反応可能な反応物質の量は反応の後期の段階において低く、したがって発熱反応の結果として温度が工程の最適な範囲を離れる危険性は低下するので、このことが可能である。結果として、プロセスガス混合物の温度を特定の組成物に対する最適温度に近く保つことができる。
段階1および2:30%
段階3および4:40%
段階5および6:50%
段階7および8:60%
段階9および10:70%
段階11および12:80%
段階13および14:90%
段階15および16:100%
段階17および18:100%
Claims (26)
- プロセスガス混合物を反応器中で少なくとも2つの別々な反応域において断熱的条件下で触媒床上で反応させ、
引き続いて少なくとも1つの反応域を出るプロセスガス混合物を特定の反応域の下流で連結されている熱交換器に通すことによる、
酸素による塩化水素の接触気相酸化により塩素を製造する方法であって、
熱交換器が、一方のプレートの上面に他方を重ねて層とされ、相互に結合されたプレートを含み、
個別のプレートが予め決め得るパターンにしたがって少なくとも2つの別々な流体流れチャンネルを有し、ならびに
プレートが、第1の流れ経路方向のプロセスガス混合物と、第2の流れ経路方向の熱交換器中で使用される熱交換媒体、が熱交換器中で流れるように配置された流体流れチャンネルを提供する
ことを特徴とする方法。 - 触媒床が構造化された充填物として構成されている、請求項1に記載の方法。
- 触媒がモノリシック触媒の形で触媒床中に存在する、請求項1に記載の方法。
- 熱交換器中の流体流れチャンネルの水力学的直径が≧10μmから≦10mm、好ましくは≧100μmから≦5mm、更に好ましくは≧1mmから≦2mmである、請求項1から3のいずれか一つに記載の方法。
- ≧6から≦50の、好ましくは≧10から≦40の、更に好ましくは≧20から≦30の反応域を含んでなる、請求項1から4のいずれか一つに記載の方法。
- 塩化水素と酸素が反応器の中に同時にフィードされる、請求項1から5のいずれか一つに記載の方法。
- 少なくとも1つの反応域の長さが≧0.01mから≦5m、好ましくは≧0.03mから≦1m、更に好ましくは≧0.05mから≦0.5mである、請求項1から6のいずれか一つに記載の方法。
- 触媒が少なくとも1つの担体と触媒活性成分/構成材料を含む、請求項1から7のいずれか一つに記載の方法。
- 触媒が反応域中の触媒活性成分/構成材料として、銅、カリウム、ナトリウム、クロム、セリウム、金、ビスマス、鉄、ルテニウム、オスミウム、ウラニウム、コバルト、ロジウム、イリジウム、ニッケル、パラジウムおよび/または白金、および上述の元素の酸化物、塩化物および/またはオキシ塩化物からなる群から選択される物質を独立に含む、請求項8に記載の方法。
- 担体が酸化チタン、酸化スズ、酸化アルミニウム、酸化ジルコニウム、酸化バナジウム、酸化クロム、酸化ウラニウム、酸化ケイ素、珪質土、炭素ナノチューブ、二酸化セリウムまたは列挙した物質の混合物または化合物、特に混合酸化物を含む、請求項8および9のいずれかに記載の方法。
- 触媒の粒子サイズが独立に≧1mmから≦10mm、好ましくは≧1.5mmから≦8mm、更に好ましくは≧2mmから≦5mmである、請求項1から10のいずれか一つに
記載の方法。 - 異なる反応域中の触媒が異なる活性を有し、反応域中の触媒の活性が好ましくはプロセスガスの流れ方向に沿って増大する、請求項1から11のいずれか一つに記載の方法。
- 固定床触媒の連続的交換が行われる、請求項1から12のいずれか一つに記載の方法。
- 第1の反応域の上流のプロセスガスの入口の絶対圧力が≧1バールから≦60バール、好ましくは≧2バールから≦20バール、更に好ましくは≧3バールから≦8バールである、請求項1から13のいずれか一つに記載の方法。
- 反応域の上流のプロセスガスの入口温度が≧250℃から≦630℃、好ましくは≧310℃から≦480℃、更に好ましくは≧330℃から≦400℃である、請求項1から14のいずれか一つに記載の方法。
- 反応域中の最高温度が≧340℃から≦650℃、好ましくは≧350℃から≦500℃、更に好ましくは≧365℃から≦420℃である、請求項1から15のいずれか一つに記載の方法。
- 直列接続の反応域が種々の平均温度で運転される、請求項1から16のいずれか一つに記載の方法。
- 反応器中のプロセスガスの滞留時間が合計≧0.5秒から≦60秒、好ましくは≧1秒から≦30秒、更に好ましくは≧2秒から≦10秒である、請求項1から17のいずれか一つに記載の方法。
- 非転化反応物質が反応器の開始点の中に戻される、請求項1から18のいずれか一つに記載の方法。
- 熱交換器中で流れる熱交換媒体が液体、沸騰液体、ガス、有機熱キャリア、塩融液および/またはイオン性液体からなる群から選択され、水、部分的に蒸発する水、および/または水蒸気を選択することが好ましい、請求項1から19のいずれか一つに記載の方法。
- 熱交換媒体と生成物流れの間の平均対数温度差が≧5Kから≦300K、好ましくは≧10Kから≦250K、更に好ましくは≧50Kから≦150Kである、請求項1から20のいずれか一つに記載の方法。
- 触媒1kg当りのCl2のkg数で表わして空間・時間収率が≧0.1から≦10、好ましくは≧0.3から≦3、更に好ましくは≧0.5から≦2であるように行われる、請求項1から21のいずれか一つに記載の方法。
- 熱交換器中で除去される反応熱が水蒸気の発生に使用される、請求項1から22のいずれか一つに記載の方法。
- 第1の反応域の中に入る前の塩化水素に対する酸素のモル比が≧0.25から≦10、好ましくは≧0.5から≦5、更に好ましくは≧0.5から≦2である、請求項1から23のいずれか一つに記載の方法。
- プロセスガスが不活性ガス、好ましくは窒素および/または二酸化炭素を含み、不活性ガスが≧15モル%から≦30モル%、好ましくは≧18モル%から≦28モル%、更に
好ましくは≧20モル%から≦25モル%のプロセスガスの比率も有する、請求項1から24のいずれか一つに記載の方法。 - 請求項1から25のいずれか一つに記載の方法によって酸素により塩化水素を接触気相酸化することによる塩素を製造するための反応器系。
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DE200710033113 DE102007033113A1 (de) | 2007-07-13 | 2007-07-13 | Temperaturstabiler Katalysator für die Chlorwasserstoffgasphasenoxidation |
DE102007033114A DE102007033114A1 (de) | 2007-07-13 | 2007-07-13 | Verfahren zur Herstellung von Chlor durch Gasphasenoxidation von Chlorwasserstoff |
DE102007033106A DE102007033106A1 (de) | 2007-07-13 | 2007-07-13 | Verfahren zur Herstellung von Chlor durch Gasphasenoxidation |
PCT/EP2008/005352 WO2009010181A1 (de) | 2007-07-13 | 2008-07-01 | Verfahren zur herstellung von chlor durch gasphasenoxidation |
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JP2014516315A (ja) * | 2011-08-17 | 2014-07-10 | アレヴァ ゲゼルシャフト ミット ベシュレンクテル ハフツング | 酸化ウラン触媒体の製造方法 |
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DE102007045123A1 (de) * | 2007-09-20 | 2009-04-02 | Bayer Technology Services Gmbh | Reaktor und Verfahren zu dessen Herstellung |
DE102008050975A1 (de) * | 2008-10-09 | 2010-04-15 | Bayer Technology Services Gmbh | Mehrstufiges Verfahren zur Herstellung von Chlor |
KR20130098871A (ko) * | 2010-04-28 | 2013-09-05 | 다우 글로벌 테크놀로지스 엘엘씨 | 다이클로린의 제조 방법 및 이를 위한 시스템 |
DE102010039734A1 (de) * | 2010-08-25 | 2012-03-01 | Bayer Materialscience Aktiengesellschaft | Katalysator und Verfahren zur Herstellung von Chlor durch Gasphasenoxidation |
CN106517095A (zh) * | 2016-09-27 | 2017-03-22 | 上海氯碱化工股份有限公司 | 制备氯气的方法 |
WO2019025967A1 (en) * | 2017-07-31 | 2019-02-07 | Sabic Global Technologies B.V. | SYSTEM AND METHOD FOR DEHYDROGENATION OF ISOBUTANE ISOBUTYLENE |
US11179703B2 (en) | 2018-02-23 | 2021-11-23 | Lg Chem. Ltd. | Catalyst for processing oxychlorination of hydrocarbon, preparation method therefor, and preparation method of oxychlorinated compound of hydrocarbon using same |
CN109453764A (zh) * | 2018-11-16 | 2019-03-12 | 西安元创化工科技股份有限公司 | 用于氯化氢氧化制氯气的二氧化钌催化剂及其制备方法 |
CN111252737A (zh) * | 2020-01-19 | 2020-06-09 | 无锡玖汇科技有限公司 | 一种用于盐酸原位制氯气的固体反应物 |
CN111056534A (zh) * | 2020-01-19 | 2020-04-24 | 无锡玖汇科技有限公司 | 一种盐酸原位制氯气的连续生产系统 |
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