WO2011152752A1 - Method for producing a coking additive by delayed coking - Google Patents

Method for producing a coking additive by delayed coking Download PDF

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Publication number
WO2011152752A1
WO2011152752A1 PCT/RU2010/000795 RU2010000795W WO2011152752A1 WO 2011152752 A1 WO2011152752 A1 WO 2011152752A1 RU 2010000795 W RU2010000795 W RU 2010000795W WO 2011152752 A1 WO2011152752 A1 WO 2011152752A1
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Prior art keywords
coking
additive
coke
chamber
raw material
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PCT/RU2010/000795
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French (fr)
Russian (ru)
Inventor
Геннадий Георгиевич ВАЛЯВИН
Николай Иванович ВЕТОШКИН
Виктор Павлович ЗАПОРИН
Сергей Витальевич СУХОВ
Михаил Владимирович МАМАЕВ
Игорь Викторович БИДИЛО
Константин Геннадьевич ВАЛЯВИН
Михаил Иванович СТУКОВ
Владимир Семенович ЗАГАЙНОВ
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Общество С Ограниченной Ответственностью "Пpomиhtex"
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Priority to CA2792300A priority Critical patent/CA2792300C/en
Priority to CN201080065694.7A priority patent/CN102892863B/en
Priority to BR112012030726A priority patent/BR112012030726A2/en
Priority to US13/701,229 priority patent/US20130276587A1/en
Priority to JP2013502520A priority patent/JP2013523942A/en
Priority to UAA201213295A priority patent/UA104526C2/en
Priority to EP10852594.0A priority patent/EP2578666B1/en
Priority to KR1020127026056A priority patent/KR20130025875A/en
Publication of WO2011152752A1 publication Critical patent/WO2011152752A1/en

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/045—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing mineral oils, bitumen, tar or the like or mixtures thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/005—Coking (in order to produce liquid products mainly)

Definitions

  • the invention relates to the field of oil refining, in particular, to a delayed coking process to produce coke with a volatile content of 15-25% for use as a coking additive in a coal coking charge in the production of metallurgical coke.
  • Petroleum coke with a volatile matter content of more than 14% and less than 25% makes it possible not only to replace the K grade coke coal (coking) for introducing coal coking into the charge, but also to improve the quality of metallurgical coke obtained (Pat. RF JY O 2355729, ⁇ 10 ⁇ 57 / 04 , published on May 20, 2009).
  • a known method of producing petroleum coke by delayed coking of the oil residue including heating the feedstock in a tubular furnace to 490 - 515 ° C, mixing the feedstock with recirculated by distillate coking products formed in the coking chamber in a distillation column with the formation of distillation residue, the supply of secondary raw materials - bottoms the remainder in the coking chamber with a temperature of 485-495 ° C and coking with the formation of coke.
  • the disadvantage of this method is that as a result of coking get high strength coke with a low content of volatile substances (up to 9%) of the mass).
  • Closest to the claimed object is a method of delayed coking of oil residue, including heating the feedstock to 340-380 ° C, mixing it with recirculate heavy coking gas oil (pyrolysis resin, heavy catalytic cracking gas oil) in a mixing tank to form secondary raw materials, heating the secondary raw materials obtained in the mixing tank of the heavy residue and fed into the coking chamber with a temperature of 485-505 ° C, coking with the formation of coke (Pat. RF N ° 2206595, class C 10B 55/00, publ. 20.06.2003).
  • heavy coking gas oil pyrolysis resin, heavy catalytic cracking gas oil
  • the disadvantage of this method is the low content of volatiles in the obtained coke due to the high coking temperature (485-505 ° C), as well as low productivity due to intensive foaming and, as a result, the inability to more fully use the volume of the coking chamber.
  • the invention is aimed at increasing the content of volatile substances in coke and increasing the productivity of the installation.
  • the secondary raw materials are fed into the coking chamber with a temperature of 455-470 ° C.
  • an anti-foam additive is fed into the coking chamber.
  • the antifoam additive is fed to two or four points along the perimeter of the coking chamber in order to completely cover the surface of the foam.
  • the implementation of the coking process at low temperatures due to the supply of raw materials at the inlet of the coking chamber with a low temperature will allow to obtain coke with a volatile content of 15-25% for use as a coking additive.
  • the supply of antifoam additives during the last 3-5 hours before the coking process is completed will not only reduce the level of foam in the coking chamber, but will also increase the productivity of the feedstock process.
  • the drawing shows a schematic diagram of an installation for implementing the proposed method for producing coking additives delayed coking.
  • the proposed method for producing coking additives delayed coking is as follows.
  • the feedstock which can be used as tar, deasphalting asphalt, oil extracts, heavy catalytic cracking gas oils or mixtures thereof in any proportions, is heated in a tube furnace 1 to a temperature of 270 - 350 ° C and fed into a mixing tank 2 connected by vapors with distillation column 3.
  • Heavy coking gas oil, withdrawn from distillation column 3 in the form of a side stream, is fed into the same container as a recirculate.
  • the resulting secondary raw material obtained by mixing the primary raw material with recirculated material is heated in a tube furnace 4 and fed to alternating coking chambers 5 with a temperature of 455-470 ° C, where the resulting coking agent accumulates, the additive with a volatile content of 15-25%.
  • the distillate coking products formed in the coking chamber 5 are fed to a distillation column 3 for separation into gas, gasoline, light and heavy coking gas oils and bottoms. Vaporous products leave on top of distillation column 3, light and heavy gas oils are removed from its middle part, and bottom residue is withdrawn from the bottom.
  • an anti-foam additive 6 is fed into the coking chamber 5 at four points around the perimeter of the chamber.
  • the proposed method is illustrated by examples 1 - 4.
  • coking of a mixture of raw materials consisting of a vacuum residue of visbreaking, tar and heavy gas oil of catalytic cracking in the ratio of 15:75: 10 was carried out.
  • the raw material has a density of 1.055 g / cm3, coking 25.8% and a sulfur content of 3.8%.
  • the primary raw material was heated in the convection section of the furnace to a temperature of 320 ° C and mixed in a mixing tank with recirculate - heavy coking gas oil, removed from the distillation column in the form of a side stream.
  • the resulting secondary raw material was heated in a tube furnace and fed into a coking chamber to obtain a coking additive.
  • the coke was steamed with water vapor, cooled with water and discharged hydraulically.
  • examples 2 and 4 to prevent foaming in the coking chamber 4 hours before the end of coking, an antifoam additive was applied.
  • the mode and results of coking in examples 1 to 4 are summarized in table.
  • coking of the same raw materials was carried out as in examples 1-4, according to the prototype, with a secondary feed temperature at the entrance to the coking chamber 485 ° C without anti-foam additives.
  • the result was a conventional electrode coke with a volatile content of 10.8%.
  • the mode and results of coking are summarized in the same table.
  • the proposed coking method will allow to obtain coke for use as a coking additive with a volatile content of more fifteen %.
  • the supply of raw materials to a chamber with a temperature below 456 ° C is impractical, since a bituminous mass may form in the upper part of the coking chamber, which causes difficulties for steaming and cooling the coke.
  • raw materials are supplied above a temperature of 470 ° C, coke is formed with a volatile matter content of less than 15%.
  • the supply of antifoam additives to the upper part of the coking chamber will reduce the level of foam formed during the coking process, which will increase the productivity of the method for feedstock.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention relates to the field of oil refining and, in particular, to a delayed coking process that produces coke with a volatile substances content of 15-25% for use as a coking additive in a coal coking charge in the production of metallurgical coke. The invention is directed towards increasing the content of volatile substances in coke and increasing the efficiency of a plant. The method comprises preheating a primary raw material, mixing the latter with recycle in a tank in order to form a secondary raw material, heating the secondary raw material to 455-470°C and supplying the latter to a coking chamber, and coking to form a coking additive. It is expedient to feed an antifoaming additive into the coking chamber 3-5 hours before coking is finished. It is preferable to feed in the antifoaming addition agent at two - four points around the perimeter of the coking chamber.

Description

Способ получения коксующей добавки замедленным коксованием  A method of obtaining a coking additive delayed coking
Изобретение относится к области нефтепереработки, в частности, к процессу замедленного коксования с получением кокса с содержанием летучих веществ 15-25 % для использования в качестве коксующей добавки в шихту коксования углей при производстве металлургического кокса. Нефтяной кокс с содержанием летучих веществ более 14 % и менее 25% дает возможность не только заменить остродефицитный уголь марки К (коксующий) для введения в шихту коксования углей, но и улучшить качество получаемого металлургического кокса (Пат. РФ JYO 2355729, С10В57/04, опубл. 20.05.2009 г.). Известен способ получения нефтяного кокса замедленным коксованием нефтяного остатка, включающий нагрев исходного сырья в трубчатой печи до 490 - 515 °С, смешивание исходного сырья с рециркулятом - образованными в камере коксования дистиллятными продуктами коксования в ректификационной колонне с образованием кубового остатка, подачу вторичного сырья - кубового остатка в камеру коксования с температурой 485-495 °С и коксование с образованием кокса. (З.И.Сюняев, «Производство, облагораживание и применение нефтяного кокса », М. Химия, 1973, с. 95). Недостаток этого способа заключается в том, что в результате коксования получают кокс высокой прочности с низким содержанием летучих веществ (до 9 %) масс). Увеличить содержание летучих веществ в коксе возможно путем снижения температуры сырья на входе в камеру коксования. Однако снижение температуры нагрева сырья и коксование при низких температурах приводит к интенсивному пенообразованию и, как следствие, к вероятности переброса пены в ректификационную колонну, а затем - в печь, что способствует закоксовыванию аппаратуры и, соответственно, снижению межремонтного пробега установки. The invention relates to the field of oil refining, in particular, to a delayed coking process to produce coke with a volatile content of 15-25% for use as a coking additive in a coal coking charge in the production of metallurgical coke. Petroleum coke with a volatile matter content of more than 14% and less than 25% makes it possible not only to replace the K grade coke coal (coking) for introducing coal coking into the charge, but also to improve the quality of metallurgical coke obtained (Pat. RF JY O 2355729, С10В57 / 04 , published on May 20, 2009). A known method of producing petroleum coke by delayed coking of the oil residue, including heating the feedstock in a tubular furnace to 490 - 515 ° C, mixing the feedstock with recirculated by distillate coking products formed in the coking chamber in a distillation column with the formation of distillation residue, the supply of secondary raw materials - bottoms the remainder in the coking chamber with a temperature of 485-495 ° C and coking with the formation of coke. (Z. I. Syunyaev, “Production, refinement and use of petroleum coke”, M. Chemistry, 1973, p. 95). The disadvantage of this method is that as a result of coking get high strength coke with a low content of volatile substances (up to 9%) of the mass). It is possible to increase the content of volatiles in coke by lowering the temperature of the raw material at the entrance to the coking chamber. However, a decrease in the heating temperature of raw materials and coking at low temperatures leads to intense foaming and, as a consequence, to the probability of foam being transferred to a distillation column and then to the furnace, which contributes to coking of the equipment and, consequently, to a decrease in the overhaul distance of the installation.
Для предотвращения вероятности попадания коксовой пены в реакционные змеевики печи, их закоксовывания и тем самым увеличения межремонтных пробегов установки, необходима специальная технология процесса замедленного коксования, исключающая при формировании вторичного сырья непосредственный контакт первичного сырья с парами, поступающими из камер коксования в ректификационную колонну. To prevent the likelihood of coke foam getting into the reaction coils of the furnace, their coking, and thereby increasing the turnaround time of the installation, a special technology of the delayed coking process is required, which excludes direct contact of the primary raw material with the vapors coming from the coking chambers into the distillation column when forming secondary raw materials.
Наиболее близким к заявляемому объекту является способ замедленного коксования нефтяного остатка, включающий нагрев исходного сырья до 340-380 °С, смешивание его с рециркулятом - тяжелым газойлем коксования (смолой пиролиза, тяжелым газойлем каталитического крекинга) в смесительной емкости для формирования вторичного сырья, нагрев вторичного сырья, полученного в смесительной емкости тяжелого остатка и подачу в камеру коксования с температурой 485-505° С, коксование с образование кокса (Пат. РФ N° 2206595, кл. С 10В 55/00, опубл. 20.06.2003 г.). Closest to the claimed object is a method of delayed coking of oil residue, including heating the feedstock to 340-380 ° C, mixing it with recirculate heavy coking gas oil (pyrolysis resin, heavy catalytic cracking gas oil) in a mixing tank to form secondary raw materials, heating the secondary raw materials obtained in the mixing tank of the heavy residue and fed into the coking chamber with a temperature of 485-505 ° C, coking with the formation of coke (Pat. RF N ° 2206595, class C 10B 55/00, publ. 20.06.2003).
Недостаток данного способа - низкое содержание летучих веществ в получаемом коксе из-за высокой температуры коксования (485-505°C), а также низкая производительность из-за интенсивного пенообразования и, как следствие, невозможности более полного использования объема камеры коксования. Изобретение направлено на повышение содержания летучих веществ в коксе и увеличение производительности установки. Это достигается тем, что в способе получения коксующей добавки замедленным коксованием, включающем предварительный нагрев исходного сырья до 270 - 350 °С, смешивание исходного сырья с рециркулятом в емкости с формированием вторичного сырья, нагрев вторичного сырья и подачу его в камеру коксования, коксование с образованием целевого продукта, согласно изобретению, вторичное сырье подают в камеру коксования с температурой 455-470 °С. Кроме того, для предотвращения пенообразования за 3-5 часов до завершения коксования в камеру коксования подают антипенную присадку. Причем, учитывая высокий слой коксовой пены, образующейся при коксовании при низких температурах, антипенную присадку с целью полного перекрытия поверхности пены подают в две-четыре точки по периметру камеры коксования. Осуществление процесса коксования при низких температурах вследствие подачи сырья на входе камеры коксования с низкой температурой позволит получить кокс с содержанием летучих веществ 15-25 % для использования в качестве коксующей добавки. Подача антипенной присадки в течение последних 3-5 часов до завершения процесса коксования обеспечит не только снижение уровня пены в камере коксования, но и позволит повысить производительность процесса по исходному сырью. На чертеже приведена принципиальная схема установки для осуществления предлагаемого способа получения коксующей добавки замедленным коксованием. Предлагаемый способ получения коксующей добавки замедленным коксованием осуществляют следующим образом. Исходное сырье, в качестве которого могут быть использованы гудрон, асфальт деасфальтизации, экстракты масляного производства, тяжелые газойли каталитического крекинга или их смеси в любых соотношениях, нагревают в трубчатой печи 1 до температуры 270 - 350 °С и подают в смесительную емкость 2, соединенную по парам с ректификационной колонной 3. В эту же емкость в качестве рециркулята подают тяжелый газойль коксования, выводимый из ректификационной колоны 3 в виде бокового погона. Получаемое в результате смешивания первичного сырья с рециркулятом вторичное сырье нагревают в трубчатой печи 4 и с температурой 455-470 °С подают в попеременно работающие камеры коксования 5, где накапливается образующаяся коксующая , добавка с содержанием летучих веществ 15-25 %. Дистиллятные продукты коксования, образовавшиеся в камере коксования 5, подают в ректификационную колонну 3 для разделения на газ, бензин, легкий и тяжелый газойли коксования и кубовый остаток. Сверху ректификационной колонны 3 уходят парообразные продукты, из средней ее части выводятся легкий и тяжелый газойли, а с низа - кубовый остаток. Для снижения пенообразования за 3-5 часов до завершения коксования в камеру коксования 5 подают антипенную присадку 6 в четыре точки по периметру камеры. Предлагаемый способ иллюстрируется примерами 1 - 4. На промышленной установке замедленного коксования было проведено коксование смеси сырья, состоящего из вакуумного остатка висбрекинга, гудрона и тяжелого газойля каталитического крекинга в соотношении 15:75: 10. Сырье имеет плотность 1 ,055 г/смЗ, коксуемость 25,8 % и содержание серы 3,8 %. Первичное сырье нагрели в конвекционной секции печи до температуры 320 °С и смешали в смесительной емкости с рециркулятом - тяжелым газойлем коксования, выводимым из ректификационной колонны в виде бокового погона. Полученное в результате смешивания вторичное сырье нагрели в трубчатой печи и подали в камеру коксования для получения коксующей добавки. По завершению цикла коксования кокс пропарили водяным паром, охладили водой и выгрузили гидравлическим способом. В примерах 2 и 4 для исключения пенообразования в камере коксования за 4 часа до завершения коксования подали антипенную присадку. Режим и результаты коксования по примерам 1 -4 сведены в таблицу. Для сравнения было осуществлено коксование того же сырья, что и в примерах 1 -4, по прототипу с температурой подачи вторичного сырья на входе в камеру коксования 485 °С без подачи антипенной присадки. В результате был получен обычный электродный кокс с содержанием летучих веществ 10,8 %. Режим и результаты коксования сведены в ту же таблицу. The disadvantage of this method is the low content of volatiles in the obtained coke due to the high coking temperature (485-505 ° C), as well as low productivity due to intensive foaming and, as a result, the inability to more fully use the volume of the coking chamber. The invention is aimed at increasing the content of volatile substances in coke and increasing the productivity of the installation. This is achieved by the fact that in the method of producing a coking additive by delayed coking, which includes preheating the feedstock to 270 - 350 ° C, mixing the feedstock with recycle in a tank with the formation of secondary raw materials, heating the secondary raw materials and feeding it into the coking chamber, coking with the formation the target product, according to the invention, the secondary raw materials are fed into the coking chamber with a temperature of 455-470 ° C. In addition, to prevent foaming 3-5 hours before coking is completed, an anti-foam additive is fed into the coking chamber. Moreover, taking into account the high layer of coke foam formed during coking at low temperatures, the antifoam additive is fed to two or four points along the perimeter of the coking chamber in order to completely cover the surface of the foam. The implementation of the coking process at low temperatures due to the supply of raw materials at the inlet of the coking chamber with a low temperature will allow to obtain coke with a volatile content of 15-25% for use as a coking additive. The supply of antifoam additives during the last 3-5 hours before the coking process is completed will not only reduce the level of foam in the coking chamber, but will also increase the productivity of the feedstock process. The drawing shows a schematic diagram of an installation for implementing the proposed method for producing coking additives delayed coking. The proposed method for producing coking additives delayed coking is as follows. The feedstock, which can be used as tar, deasphalting asphalt, oil extracts, heavy catalytic cracking gas oils or mixtures thereof in any proportions, is heated in a tube furnace 1 to a temperature of 270 - 350 ° C and fed into a mixing tank 2 connected by vapors with distillation column 3. Heavy coking gas oil, withdrawn from distillation column 3 in the form of a side stream, is fed into the same container as a recirculate. The resulting secondary raw material obtained by mixing the primary raw material with recirculated material is heated in a tube furnace 4 and fed to alternating coking chambers 5 with a temperature of 455-470 ° C, where the resulting coking agent accumulates, the additive with a volatile content of 15-25%. The distillate coking products formed in the coking chamber 5 are fed to a distillation column 3 for separation into gas, gasoline, light and heavy coking gas oils and bottoms. Vaporous products leave on top of distillation column 3, light and heavy gas oils are removed from its middle part, and bottom residue is withdrawn from the bottom. To reduce foaming, 3-5 hours before coking is completed, an anti-foam additive 6 is fed into the coking chamber 5 at four points around the perimeter of the chamber. The proposed method is illustrated by examples 1 - 4. At an industrial delayed coking unit, coking of a mixture of raw materials consisting of a vacuum residue of visbreaking, tar and heavy gas oil of catalytic cracking in the ratio of 15:75: 10 was carried out. The raw material has a density of 1.055 g / cm3, coking 25.8% and a sulfur content of 3.8%. The primary raw material was heated in the convection section of the furnace to a temperature of 320 ° C and mixed in a mixing tank with recirculate - heavy coking gas oil, removed from the distillation column in the form of a side stream. The resulting secondary raw material was heated in a tube furnace and fed into a coking chamber to obtain a coking additive. At the end of the coking cycle, the coke was steamed with water vapor, cooled with water and discharged hydraulically. In examples 2 and 4, to prevent foaming in the coking chamber 4 hours before the end of coking, an antifoam additive was applied. The mode and results of coking in examples 1 to 4 are summarized in table. For comparison, coking of the same raw materials was carried out as in examples 1-4, according to the prototype, with a secondary feed temperature at the entrance to the coking chamber 485 ° C without anti-foam additives. The result was a conventional electrode coke with a volatile content of 10.8%. The mode and results of coking are summarized in the same table.
Таблица Сравнительные данные по коксованию сырья предлагаемым способом и способом по прототипу  Table Comparative data on the coking of raw materials by the proposed method and method according to the prototype
Figure imgf000008_0001
Figure imgf000008_0001
Как видно из представленных в таблице данных, предлагаемый способ коксования позволит получать кокс для использования в качестве коксующей добавки с содержанием летучих веществ более 15 %. Подача сырья в камеру с температурой ниже 456 °С нецелесообразна, так как в верхней части камеры коксования может образоваться битуминозная масса, которая вызывает затруднения для проведения пропарки и охлаждения кокса. При подаче же сырья выше температуры 470 °С образуется кокс с содержанием летучих веществ менее 15 %. Подача антипенной присадки в верхнюю часть камеры коксования снизит уровень пены, образующейся в процессе коксования, что позволит увеличить производительность способа по исходному сырью. As can be seen from the data presented in the table, the proposed coking method will allow to obtain coke for use as a coking additive with a volatile content of more fifteen %. The supply of raw materials to a chamber with a temperature below 456 ° C is impractical, since a bituminous mass may form in the upper part of the coking chamber, which causes difficulties for steaming and cooling the coke. When raw materials are supplied above a temperature of 470 ° C, coke is formed with a volatile matter content of less than 15%. The supply of antifoam additives to the upper part of the coking chamber will reduce the level of foam formed during the coking process, which will increase the productivity of the method for feedstock.

Claims

Формула изобретения Claim
1. Способ получения коксующей добавки замедленным коксованием, включающий предварительный нагрев исходного сырья до 270-330 °С, смешивание исходного сырья с рециркулятом в емкости с формированием вторичного сырья, нагрев вторичного сырья и подачу его в камеру коксования, коксование с образованием целевого продукта, отличающийся тем, что вторичное сырье подают в камеру коксования с температурой 455-470 °С. 1. A method of producing a coking additive by delayed coking, including preheating the feedstock to 270-330 ° C, mixing the feedstock with recycle in a tank with the formation of secondary feedstock, heating the secondary feedstock and feeding it into the coking chamber, coking with the formation of the target product, characterized the fact that the secondary raw materials are fed into the coking chamber with a temperature of 455-470 ° C.
2. Способ по п.1 , отличающийся тем, что за 3-5 часов до завершения коксования в камеру коксования подают антипенную присадку. 2. The method according to claim 1, characterized in that 3-5 hours before the end of coking in the coking chamber serves antifoam additive.
3. Способ по п.1 отличающийся тем, что антипенную присадку подают в две-четыре точки по периметру камеры коксования. 3. The method according to claim 1, characterized in that the antifoam additive is supplied at two to four points along the perimeter of the coking chamber.
PCT/RU2010/000795 2010-06-01 2010-12-28 Method for producing a coking additive by delayed coking WO2011152752A1 (en)

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BR112012030726A BR112012030726A2 (en) 2010-06-01 2010-12-28 method for producing a coke additive by delayed coking
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RU2560442C2 (en) * 2013-11-18 2015-08-20 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Method for obtaining of coking additive by slow coking
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