SU626111A1

SU626111A1 - Method of producing olefinic hydrocarbons

Info

Publication number: SU626111A1
Application number: SU762381385A
Authority: SU
Inventors: Раиль Бакирович Валитов; Хабиб Миначевич Миначев; Роберт Аветисович Караханов; Раис Рахматуллович Хабибуллин; Борис Ефимович Прусенко; Георгий Митрофанович Панченков; Дилюс Лутфуллич Рахманкулов; Николай Данилович Абалмасов; Владимир Иванович Голованов; Людмила Сергеевна Ефремова
Original assignee: Уфимский Нефтяной Институт; Московский Институт Органической Химии Ан Ссср Имени Н.Д.Зелинского
Priority date: 1976-07-01
Filing date: 1976-07-01
Publication date: 1978-09-30

Description

Изобретение относитс к нефтехимии, конкретно к области получени олефиновых углеводородов.The invention relates to petrochemistry, specifically to the field of olefinic hydrocarbon production.

Известен способ получени олефиновых углеводородов пиролизом углеводородного сырь в присутствии вод ного пара и катализатора - станната кали 1.A method of producing olefinic hydrocarbons is known by pyrolysis of a hydrocarbon feedstock in the presence of water vapor and a catalyst, potassium stannate 1.

Недостатком известного способа вл етс относительно невысокий выход целевых продуктов ( 60 %).The disadvantage of this method is the relatively low yield of the target products (60%).

Более близким к предложенному по сущности и достигаемому результату вл етс способ получени олефинов с использованием железохромкалиевого катализатора 2.Closer to the essentially proposed and achieved result is a method for producing olefins using an iron-potassium catalyst 2.

Данный способ позвол ет получать олефинов до 70 вес. %.This method allows olefins to be produced up to 70 wt. %

Недостатком известного способа вл етс невозможность получени значительных количеств олефинов без рециркул ции части сырь .The disadvantage of this method is the impossibility of obtaining significant quantities of olefins without recycling a part of the feedstock.

Цель предлагаемого изобретени - повышение выхода олефиновых углеводородов .The purpose of the present invention is to increase the yield of olefinic hydrocarbons.

Поставленна цель достигаетс за счет того, что используют катализатор, содержащий 7,0-20 вес. % окиси хрома и 80- 93 вес. % окиси железа.This goal is achieved due to the use of a catalyst containing 7.0-20 wt. % chromium oxide and 80-93 weight. % iron oxide.

Исследовани , проведенные в услови х опытных установок, позволили исключить недостатки известного способа, сохранив его преимущество.The studies carried out under the conditions of the pilot plants, made it possible to eliminate the disadvantages of this method, while retaining its advantage.

Высокий выход олефинов сохран етс . Катализатор в процессе длительной эксплуатации не требует регенерации и обладает хорошей механической прочностью. Возможно проведение процесса с полнымA high yield of olefins is maintained. The catalyst during long-term operation does not require regeneration and has good mechanical strength. It is possible to conduct the process with complete

превращением сырь .the transformation of raw materials.

Исследовани осуществл ют на укруппенной опытной установке в реакторе соThe studies were carried out on a group pilot plant in a reactor with

стационарным слоем катализатора (5 кг),fixed bed catalyst (5 kg),

наход щегос в изотермических услови хfound in isothermal conditions

(внешний обогрев). В качестве исходного сырь берут газовый бензин с н. к. 38°С и к. к. 160°С, содержащий до 80 вес. % углеводородов СБ. Концентраци ароматических углеводородов не превышает 1 %(external heating). As a feedstock take gas gasoline with n. to. 38 ° C and to. to. 160 ° C, containing up to 80 weight. % hydrocarbon sat. The concentration of aromatic hydrocarbons does not exceed 1%

(0,8 вес. %).(0.8 wt.%).

Claims

The experiments were carried out at 720-780 ° C, a mass gasoline feed rate of 1.5-2.5 g / g hour and 100 weight. % dilution of raw materials with steam in the presence of an iron oxide – chromic catalyst containing 80–93 wt. % RegOZ n 7-20 weight. % Of CO2, showed the possibility of the process. With almost complete conversion of raw materials and the output of ethylene 50-55 weight. % of raw materials. Example 1. The conditions of irocees are given below. The catalyst is an iron oxide chromium weight. % 80.5, iron oxide, 19.5 chromium oxides Raw materials Gasoline (n. To 38 ° C, k. K. 160 ° C) Process temperature, ° C 740 Raw material dilution with water vapor,% by weight 100 , g / g-h 2.0 Process indicators: Ethylene yield on raw materials, wt. % 52.8 Raw material conversion,% 100 Example

2. Process conditions: Oxide iron-chromic catalyst, weight. %: 88.5 iron oxide, 11.5 chromium oxide Gas gasoline (n. To 33 ° C, because K. 160 ° C) 780 Process temperature, ° C Dilution of the raw material with water vapor,% by weight100 g / g-p2.5 Example

3. The process is carried out on a pilot plant of a flow type with a stationary layer of an iron-chromium catalyst (50 kg of catalyst containing 87.3% iron oxide and 12.7% chromium oxide) using gasoline as a raw material (n. K. 40 ° C, k. K. 160 ° C) and containing 13.6 wt. % aromatics. Conditions of the experiment: Temperature, ° С720 Gasoline feed rate, g / h2.0 Dilution of raw materials with water vapor, weight. % 100 Process indicators: Output on raw materials, weight. %: ethylene 31.5 propylene 26.4 olefins C4 15.3 S-olefins 73.1 Conversion rate of non-aromatic part of raw material,% 100 Aromatic part yield, wt. % of raw materials 13.1 Aromatics concentration, wt. % 99.1 The yield for raw materials is calculated on the condition that the non-aromatic part is taken as 100%. This is due to the fact that under the conditions of carrying out the process on an iron-chromium catalyst, the transformation of aromatic hydrocarbons is practically not observed and can be considered as an inert component. Example

4. Experimental conditions are analogous to example 1, with the difference that a catalyst containing 3 wt. % iron oxide and 18.7 wt. % okikhroma. Conditions of the experiment: Temperature, ° С740 Feed rate of the raw material, g / h1.7 Raw material dilution with water vapor, weight. % 100 Process indicators: Output on raw materials, weight. % ethylene 37.8 propylene 22.4 olefins C4 12.7 E-olefins, 72.9 Conversion rate of the non-aromatic part of the feed,% 100 Aromatic part yield, wt. % of raw materials 13.0 Concentration, aromatics, weight. % 99.4 Process indicators: Ethylene yield on raw materials. weight. % Conversion of raw materials,% Process conditions: Example 6. Oxide iron-chromic catalyst, wt. %: 92.8 iron oxide and 7.2 chromium oxide Gasoline (n 38 ° C, ref. 160 ° C) Process temperature, ° C 760 Raw material dilution with steam,% by weight Feed rate, Process indicators : Ethylene yield on raw materials, Raw material conversions,% The catalysts under test are iron-iron and, according to materials, have a strength of 48.4 kg / cm and 3 kg / cm, respectively. After a run of optimal conditions (for 1 month), the strength of the iron-chromium catalysts is reduced to 34.5 kg / cm, while at the applied level it remains at the same level. DETAILED DESCRIPTION OF THE INVENTION A method for producing olefinic hydrocarbons by pyrolysis of hydrocarbon syes in the presence of water vapor and a catalyst containing iron and ohm compounds, characterized in that, in order to increase the yield of the target products, a catatizer containing 7.0-20.0 . % okikhroma and 80-93 weight. % iron oxide,

56

Sources of information, No. 487927, CL. From 10G 11/26, 1974.

taken into account in the examination2. “Petrochemistry, 1972, 12, No. 3, p. 3491. USSR author's certificate 352.

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