SU694483A1 - Method of refining halohydrocarbon by-products in production of allyl chloride and methallyl chloride - Google Patents
Method of refining halohydrocarbon by-products in production of allyl chloride and methallyl chlorideInfo
- Publication number
- SU694483A1 SU694483A1 SU782621764A SU2621764A SU694483A1 SU 694483 A1 SU694483 A1 SU 694483A1 SU 782621764 A SU782621764 A SU 782621764A SU 2621764 A SU2621764 A SU 2621764A SU 694483 A1 SU694483 A1 SU 694483A1
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- SU
- USSR - Soviet Union
- Prior art keywords
- chloride
- products
- production
- halohydrocarbon
- refining
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Изобретение отноеитс к области промышленного нроизводетва нефтехимических продуктов, конкретно к способу утилизации отходов производства хлорорганических продуктов.The invention relates to the field of industrial production of petrochemical products, specifically to the method of disposal of waste production of organochlorine products.
Существующие в насто щее врем производства хлоролефинов и хлоралканов практически не предусматривают возможность квалифицированного использовани образующихс в процессе побочных продуктов , таких как третичный бутилхлорид в производстве металлилхлорида и хлорнропены в производстве хлористого аллила, количество которых составл ет 0,1-0,3 т/т готового продукта. Поэтому такие побочные продукты сжигаютс с образованием хлористого водорода м углекислого газа.The currently existing production of chlorolefins and chloroalkanes practically do not provide for the qualified use of the by-products formed during the process, such as tertiary butyl chloride in the production of metal chloride and chlornropenes in the production of allyl chloride, the amount of which is 0.1-0.3 t / t product. Therefore, such by-products are burned to form hydrogen chloride and carbon dioxide.
Учитыва все возрастающий дефицит углеводородного сырь , переработка крупнотоннажных отходов хлорорганических продуктов в углекислоту представл етс крайне нерациональной, поскольку св зана с потерей углеводородной части отходов.Taking into account the growing shortage of hydrocarbon raw materials, the processing of large-tonnage organochlorine wastes into carbon dioxide is highly inefficient, since it is associated with the loss of the hydrocarbon portion of the waste.
Известен способ переработки побочных продуктов производства галоидуглеводородов , содержащих 2 атомов хлора, путем их восстановлени в газовой фазе в присутствии катализаторов гидрировани 1.A method of processing by-products of the production of halocarbons containing 2 chlorine atoms is known, by reducing them in the gas phase in the presence of hydrogenation catalysts 1.
Процесс провод т при 150-160° С. В качестве катализаторов используют 0,1-The process is carried out at 150-160 ° C. As catalysts, 0.1-
5 вес. % металлов группы платины, нанесенных на окись алюмнни или окись железа , или окись хрома, или активированный уголь.5 wt. % of platinum group metals deposited on aluminum oxide or iron oxide, or chromium oxide, or activated carbon.
Известен также способ переработки галоидуглеподородов , таких как дихлорпропан в пропан и пропилеи, дихлорбутен в бутан, хлорбензол в циклогексан, путем пидрирован1 при 50-500° С в присутствии катализаторов на основе роди 2.There is also known a method for processing halocarbons, such as dichloropropane in propane and propylene, dichlorobutene in butane, chlorobenzene in cyclohexane, by fermentation1 at 50-500 ° C in the presence of rhodium-2 based catalysts.
Кроме роди , катализатор содержит палладий, платину, рутений, железо, кобальт , никель, медь, золото, ванадий, хром, молибден, вольфрам и добавки гидроокисей НЛП карбонатов щелочных или щелочноземельных металлов и/или солей -или окислов алюмини , бора или титана.In addition to rhodium, the catalyst contains palladium, platinum, ruthenium, iron, cobalt, nickel, copper, gold, vanadium, chromium, molybdenum, tungsten and additives of NLP hydroxides of alkali or alkaline earth metals and / or salts of aluminum, boron or titanium oxides.
Иедостатком указанных способов вл етс использование катализаторов на основе дорогосто щих и дефицитных благородных металов.The disadvantage of these methods is the use of catalysts based on expensive and scarce precious metals.
Способ переработки побочных галоидуглеводородов производства хлористого аллила и металлилхлорида, таких как третичный бути тхлорид ,и хлорпропан в литературе не описаи.A method for processing side halohydrocarbons produced by allyl chloride and methyl chloride, such as tertiary buty thichloride, and chloropropane are not described in the literature.
Цель изобретени - разработка способа переработки побочных галоидуглеводородов производства хлористого аллила и м ета л л и л хлор и д а.The purpose of the invention is to develop a method for processing side halohydrocarbons to produce allyl chloride and methanol and chlorine and d.
Поставленна цель достигаетс описываемым способом переработки побочных галюидуглеводородов производства хлористого аллила ,н металлилхлорида путем гидрировапи при 160-285° С в присутствии катализатора - алюмож лезного коптакта, содержащего 10-20 вес. % оксида железа и 80-90 вес. % окиси алюмини .This goal is achieved by the described method of processing side-halyid hydrocarbons produced by allyl chloride and metal chloride by hydrogenation at 160–285 ° C in the presence of a catalyst — an aluminum alloy containing 10–20 wt. % iron oxide and 80-90 weight. % alumina.
Используемый в описываемом способе катализатор получают совместным осаждением солей алюмини и железа с последуюш им формованием, сушкой и прокалкой при 800° С в течение 3 ч. Готовый катализатор содержит от 10 до 20 вес. % оксидов железа н 80-90 вес. % окиси алюмини .The catalyst used in the described method is obtained by the joint precipitation of aluminum and iron salts, followed by molding, drying and calcining at 800 ° C for 3 hours. The finished catalyst contains from 10 to 20 weight. % iron oxide n 80-90 weight. % alumina.
Процесс провод т на установке проточного типа ео стационарным слоем катализатора массой 15 г при 160-285° С, скорости подачи сырь 0,5-1,0 г/г ч.The process is carried out on a flow-type plant eo with a stationary catalyst bed weighing 15 g at 160-285 ° C, feed rates of 0.5-1.0 g / g h.
Сырье подают шприцевым дозатором в смеситель, куда поступает водород. Смесь исходных продуктов после смесител поступает в реактор. Реакционную массу охлаждают дл конденсации и анализируют хроматограф ическнм методом.Raw materials are fed with a syringe dispenser to a mixer where hydrogen is fed. The mixture of initial products after the mixer enters the reactor. The reaction mass is cooled for condensation and the chromatograph is analyzed by a chemical method.
Пример 1. Сырье - 1- и 2-хлорпропены .Example 1. Raw materials - 1- and 2-chloropropenes.
Катализатор - 10 вес. % окиси железа, 90 вес. % окиси алюмини .Catalyst - 10 wt. % iron oxide, 90 wt. % alumina.
Услови опыта: катализатор 15 г, температура 285° С, мольный избыток водорода 1,5; скорость подачи сырь . 0,8 г/г ч; пропущено сырь за 2 ч 24 г. Результаты опытов. Получено продуктов реакции 23,4 г; конверси сырь 96 мае. %; содержание углеводородов (пропан + иропилен) в продуктах реакции без НС1 99,5 мае. %.Test conditions: catalyst 15 g, temperature 285 ° С, molar excess of hydrogen 1.5; feed rate 0.8 g / g h; missing raw materials for 2 h 24 g. The results of the experiments. The obtained reaction products 23.4 g; raw materials conversion 96 May. %; hydrocarbon content (propane + propylene) in the reaction products without HC1 99.5 May. %
Пример 2. Сырье - третичный бутилхлорид . Катализатор - 20 вес. % окиси железа, 80 вес. % окиои алюмини .Example 2. Raw materials - tertiary butyl chloride. Catalyst - 20 wt. % iron oxide, 80 wt. % aluminum oxide.
Услови опыта: масса катализатора 15 г; температура 160° С, мольный избыток кислорода 0,7; скорость подачи сырь 0,5 г/г ч; нропущеио сырь за 2 ч 15 г. Test conditions: catalyst weight 15 g; temperature 160 ° C, molar excess oxygen of 0.7; feed rate of 0.5 g / g; Unsuspected raw materials for 2 hours and 15 g.
Результаты опытов. Получено продуктовThe results of the experiments. Products received
реакции 14,7 г; конверси сырь 98 мае. %;reactions of 14.7 g; raw material conversion 98 May. %;
содержание углеводородов (изобутилен,hydrocarbon content (isobutylene,
изобутан) в продуктах реакции без НС1isobutane) in the reaction products without HC1
99,1 мае. %.99.1 May. %
Таким образом, иро;длагаемый способ позвол ет квалифицированно использовать побочные продукты производства хлорорга}1ических соединений нутем регенерации углеводородной части отходов в углеводороды (изобутилен, изобутан, иропан, нроиилен ), которые могут быть вновь использованы в процессах нефтехимического синтеза . При этом исключаетс использование дорогосто щих катализаторов гидрировани на основе благородных металлов.Thus, the advanced method allows qualified use of the by-products of the production of chlorine} 1ic compounds by regenerating the hydrocarbon portion of the waste into hydrocarbons (isobutylene, isobutane, propane, niroiylene), which can be reused in petrochemical synthesis processes. This eliminates the use of expensive hydrogenation catalysts based on noble metals.
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SU782621764A SU694483A1 (en) | 1978-05-22 | 1978-05-22 | Method of refining halohydrocarbon by-products in production of allyl chloride and methallyl chloride |
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SU782621764A SU694483A1 (en) | 1978-05-22 | 1978-05-22 | Method of refining halohydrocarbon by-products in production of allyl chloride and methallyl chloride |
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US8198495B2 (en) | 2010-03-02 | 2012-06-12 | Marathon Gtf Technology, Ltd. | Processes and systems for the staged synthesis of alkyl bromides |
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US8815050B2 (en) | 2011-03-22 | 2014-08-26 | Marathon Gtf Technology, Ltd. | Processes and systems for drying liquid bromine |
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- 1978-05-22 SU SU782621764A patent/SU694483A1/en active
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US8173851B2 (en) | 2004-04-16 | 2012-05-08 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons |
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US8198495B2 (en) | 2010-03-02 | 2012-06-12 | Marathon Gtf Technology, Ltd. | Processes and systems for the staged synthesis of alkyl bromides |
US8815050B2 (en) | 2011-03-22 | 2014-08-26 | Marathon Gtf Technology, Ltd. | Processes and systems for drying liquid bromine |
US8436220B2 (en) | 2011-06-10 | 2013-05-07 | Marathon Gtf Technology, Ltd. | Processes and systems for demethanization of brominated hydrocarbons |
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