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WO2009022937A1 - Procédé de craquage thermique de produit d'huile lourde - Google Patents

Procédé de craquage thermique de produit d'huile lourde Download PDF

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Publication number
WO2009022937A1
WO2009022937A1 PCT/RU2007/000433 RU2007000433W WO2009022937A1 WO 2009022937 A1 WO2009022937 A1 WO 2009022937A1 RU 2007000433 W RU2007000433 W RU 2007000433W WO 2009022937 A1 WO2009022937 A1 WO 2009022937A1
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WO
WIPO (PCT)
Prior art keywords
oil product
residue
heating furnace
furnace
consumption
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/RU2007/000433
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English (en)
Inventor
Aleksandr Ivanovich Leonov
Igor Nickolaevich Andreichuk
Pavel Evgenievich Portnov
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Individual
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Individual
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Filing date
Publication date
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Priority to PCT/RU2007/000433 priority Critical patent/WO2009022937A1/fr
Publication of WO2009022937A1 publication Critical patent/WO2009022937A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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

Definitions

  • the invention refers to oil refining, in particular, to production of hydrocarbon fuel in oil-refining industry.
  • thermal cracking (Dekhterman A.Sh. Oil refining by a fuel variant. M., Khimiya, 1988. p.47).
  • thermal cracking e.g., in the two-coil processing solution
  • high-boiling distillate or residual stock is processed into gas, gasoline, unsaturated hydrocarbons (ethylene, butenes, propylene), gas oil and cracked residue.
  • Obtained cracked gasolines differ considerably from straight-run gasolines, as the former have higher contents of unsaturated and aromatic hydrocarbons, as well as paraffin hydrocarbons of isometric structure. Due to presence of the aforesaid hydrocarbons, cracked gasolines are characterized with higher antiknock properties, compared to straight-run gasolines.
  • Gas oil in terms of its breakup, corresponds to the kerosene-gas oil cut and is used as a component of fuel oil. Cracked residue contains resinous substances, asphaltenes and carboides.
  • Heavy-oil products fuel oil, tar — are most easily destroyed, when heated.
  • the most important parameters, which determine direction and rate of cracking, are temperature, duration of process and pressure.
  • thermolysis of gaseous light or middle-distillate stock may have the process temperature reaching 750 ⁇ 800 °C.
  • the thermolysis products would mostly be constituted by naphtheno-aromatic structures, which would hinder further consolidation reactions.
  • thermolysis requires certain duration.
  • Pressure affects composition of the process products (e.g. output of residual cuts and coke) due to changing rates and nature of secondary reactions of 0 polymerization and condensation, as well as volume of reacting mixture). Polymerization and condensation run faster at higher pressure. With growth of pressure, gas formation is reduced, and more gasoline is obtained, with a smaller W
  • the process conditions - temperature, pressure and duration of the process - are specified individually for each particular case.
  • the depth of stock conversion in a single run of the heater is limited by its coking.
  • the flow chart and equipment for further process are developed, accordingly.
  • the patent also describes a device for implementation of the aforesaid method. It comprises a
  • heating furnace with a coil and a remote soaking chamber.
  • a throttling reactor in the form of a flow resistor, which provides for pressure relief at the outlet of the heating furnace and delivery of homogenous additives to the reaction zone of the remote soaking chamber for intensification of the process of deepening thermal cracking of heavy-oil products.
  • Adjustment of the process duration is related to the stock consumption, or its flow rate. Reduction of the rate of stock flow in the coil raises the probability of coke formation on the coil walls. Changing the length of the heating zone (coil length) requires the furnace design to be modified.
  • the known method is implemented as follows.
  • the stock comes to furnace P- 1 and passes through it in two streams up to a specified conversion level, that is, with a certain number of cracking products to be obtained.
  • the vapors of cracking products are fed to evaporator K-2, from the bottom of which cracked residue is output, with the vapors going to rectifying column K-3.
  • Gasoline vapors and gas are driven out from the top of the column.
  • the "rich" gas is separated from unstable gasoline in gas separator S-I.
  • the diesel cut is removed from the middle section of column K-3 through stripping column K-I.
  • the rectified residue is returned from column K-3 to furnace P-I to be recirculated.
  • the amount of recirculated product does not exceed 25 % of the feed stock consumption.
  • the remaining products of the process are removed from the bottom of column K-2.
  • the temperature at the outlet of furnace P-I is 480 ⁇ 485 °C.
  • a cooling stream of oil product is introduced into the line of the product outgoing from furnace P-I.
  • the level of its conversion is limited to prevent formation of carbenes and carboids. This is achieved through reducing the reaction duration.
  • the processing chart docs not provide for installation of an additional soaking chamber and the second furnace (deep cracking furnace). At the same time, the output of products is not high.
  • thermal cracking units the amount of output products should be higher, as these are target products. To this effect, it is necessary to extend the period of stock exposure at the process temperature, or directly in the furnace, by means of increasing the coil length, or exposing the products in an additional soaking chamber to be installed downstream the furnace, according to the oil product flow. Operation of thermal cracking units is characterized by a short trouble-free period, which sometimes does not exceed 20 days (ibid. p. 51).
  • the technical objective of the invention is creation of an. efficient method of thermal cracking of heavy-oil products, which could expand possibilities of application of thermal cracking in industry.
  • the technical result to ensure reaching the set problem lies in raising controllability of the thermal cracking process, extending the range of adjustment of the process parameters and, respectively, versatility and efficiency of the method.
  • the essence of the invention is that the method of thermal cracking of heavy- oil products provides for that a stream of oil products outgoing from the heating furnace is supplied with a stream of the source oil product, whereupon they are jointly fed to a throttling device used for maintaining required pressure in the heating furnace, whereupon the liquid-vapor mixture formed as a result of throttling is delivered to a low pressure separator, from the bottom of which the heavy cracked residue is removed in two directions: the smaller flow would go as the process product, and the bigger flow would go through an intermediate container to return to the heating furnace, while from the upper part of the separator the light cuts are delivered to a rectifying column, from which are removed the cuts of cracked products of required composition and the rectification residue, which is fed to the aforesaid intermediate container for return to the heating furnace jointly with the separation residue, with the aggregate consumption
  • the liquid- vapor mixture which, upon being cooled, comes to the gas separator, where it is divided into gas, water and gasoline cut, one part of which is used to reflux the top of the low pressure separator, and the other part is recovered for the process to follow — stabilization, with the light gas oil cut concurrently removed through the stripping column.
  • a heavy-oil product (fuel oil or tar) is used as the stock oil product
  • a pipe furnace being used as a heating furnace, where to prevent coke deposits from building up on the furnace coil walls, the coil is supplied with a baffle, e.g. water steam, the intermediate container is supplied with additives of the physical-chemical nature to activate the thermal cracking process, while the residue is returned from the intermediate .container to the furnace with a flow rate exceeding consumption of the stock oil product with a factor of 8 to 12.
  • the process of thermal cracking to a required level of conversion of the input stock is going on fractionally, as the same oil product is delivered successively to the cracking zone (heating furnace coil) and to the zone of thermolysis products separation. After that, it is again returned from the separation zone to the input of the cracking zone.
  • the duration of the oil product exposure in the cracking zone (furnace coil) in a single run may be reduced. Accordingly, the level of conversion of the feed stock in a single run makes a part of its required target value.
  • the share of the conversion level as related to its target value is set in the same proportion as the ration of consumption of input stock to consumption of the oil product residue returned to the cracking zone.
  • thermal cracking parameters - the process aggregate duration and temperature - are not rigidly interrelated.
  • Pressure in the heating zone may be maintained at a required level through a known method, e.g., by means of throttling the flow with a predetermined and adjustable value of pressure differential.
  • the feed stock is delivered to the hot stream of oil products downstream the heating zone, but upstream the throttling z.one.
  • the separation residue is removed from the process out of the separation zone.
  • Light thermolysis products are delivered for rectification to be separated, e.g., into gas non- condensable in the cooler, gasoline cut, light gas oil and the residue of rectification process, which is returned to the heating zone input mixed with the separation residue.
  • Fig. 1 presents curves of changes in concentration of bases of distillate cracked residue of Krasnovodsk Oil Refinery as related to thermolysis duration at the pressure of 0.1 MPa and the temperature of 420 0 C .
  • Fig. 2 presents curves of changes in concentration of bases of distillate cracked residue of Krasnovodsk Oil Refinery as related to thermolysis duration at the pressure of 0.1 MPa and the temperature of 490 °C.
  • Fig. 3 presents a simplified diagram of the visbreaking unit for implementation of the prototype method integrated in the GK-3/1 combined industrial plant. (Dekhterman A.Sh. Oil refining by a fuel variant. M., Khimiya, 1988. p.52)..
  • Fig. 4 presents a simplified flow chart of installation for implementation of the claimed method of thermal cracking of heavy-oil products.
  • the installation according to Fig.4 comprises heating furnace 1 (e.g., pipe furnace), throttling device 2, low pressure separator 3, intermediate container 4, rectifying column 5, heat exchanger 6, gas separator 7 and stripping column 8.
  • heating furnace 1 e.g., pipe furnace
  • throttling device 2 e.g., pipe furnace
  • low pressure separator 3 e.g., pipe furnace
  • intermediate container 4 e.g., pipe container
  • rectifying column 5 e.g., heat exchanger 6
  • gas separator 7 e.g., gas separator 7
  • the feed stock (stream I) is delivered to the stream of the oil product outgoing from heating furnace 1 , with the stock oil product stream fed up to throttling device 2, which is used for maintaining a required pressure of the process in heating furnace 1.
  • throttling device 2 which is used for maintaining a required pressure of the process in heating furnace 1.
  • the coil is supplied with a baffle, e.g. water steam (VII).
  • VI water steam
  • the liquid-vapor mixture is delivered to low pressure separator 3, from the bottom of which the heavy cracked residue is removed from the process (stream IV). From the lower part of separator 3, through intermediate container 4, the same residue is also removed to be returned to heating furnace 1 with a flow rate exceeding the feed stock consumption with a factor of at least two.
  • the residue of rectification process (high-boiling part of light cuts) is delivered to intermediate container 4. If necessary, this container is also supplied with additives (stream VIII) of the physical-chemical nature to activate the thermal cracking process.
  • stream VIII additives of the physical-chemical nature to activate the thermal cracking process.
  • the balance of material streams should be as follows. The total of the streams removed from the process - gasoline cut (stream II), light gas oil (stream III), heavy residue (stream IV), non-condensable hydrocarbon gases (stream V) - must be equal (by weight) to the feed stock flow (stream I).
  • control over technological parameters of the thermal cracking process subject to the claimed method is flexible in terms of setting the process parameters: its duration, temperature and pressure, as well as versatility in respect of properties of feed stock and specifying properties of products to be obtained. This allows working on the same plant with various feed stock, process it under optimum process conditions and obtain as a result a required conversion level and desired composition of thermal cracking products.
  • the claimed method was tried on a laboratory pilot plant. Fuel oil of the M-
  • the results of thermal treatment were obtained under the following specified technological parameters of the process: the temperature at the outlet of the heating furnace (furnace 1) was 440 0 C, with the absolute pressure in separator 3 maintained at the level of 0.12 MPa; the ratio of consumptions of the returned separation residue and the feed stock was set as 12:1.
  • the aggregate conversion level was obtained for thermolysis products having the end boiling point lower than 360 0 C, as calculated for feed stock in the amount of 43.5 % of weight: non-condensable gas - 3 % of weight, gasoline cut — 8.5 % of weight, kerosene-gas oil cut — 32 % of weight.
  • the separation residue with density being 1050 kg/m 3 is suitable, by its composition, as a source material for obtaining bitumen. Meanwhile, the level of conversion of the oil product passing through the furnace coil was less than 3 % of weight. This makes it possible to raise considerably the trouble-free life of the furnace.
  • the present invention is embodied with multipurpose equipment extensively employed by the industry.

Landscapes

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

Abstract

L'invention concerne un procédé de craquage thermique d'huile lourde prévu pour qu'un flux d'huile sortant du four de chauffage soit alimenté en flux d'huile source, après quoi ils sont conjointement acheminés vers un dispositif d'étranglement utilisé pour maintenir une pression requise dans le four de chauffage, après quoi le mélange de liquide-vapeur formé suite à l'étranglement est fourni à un séparateur basse pression, à partir du fond duquel le résidu craqué lourd est enlevé dans deux directions : l'écoulement plus petit passera en tant que produit de traitement, et l'écoulement plus grand passera à travers un conteneur intermédiaire pour retourner au four de chauffage, alors qu'à partir de la partie supérieure du séparateur les coupes légères sont envoyées à une colonne de rectification, à partir de laquelle sont enlevées les coupes de produits craqués ayant une composition requise et le résidu de rectification, qui est acheminé vers le conteneur intermédiaire mentionné ci-dessus pour retourner au four de chauffage conjointement avec le résidu de séparation, la consommation en agrégat dépassant la consommation d'huile de base d'un facteur d'au moins deux, où le niveau de conversion de cette huile dans la bobine du four de chauffage est fixé dans la même proportion à sa valeur cible sous forme du rapport de consommation de l'huile source sur la consommation du résidu renvoyé dans le four pour être craqué. Par conséquent, la même huile est fournie de manière répétée successivement à la zone de craquage et à la zone de séparation de produits de craquage thermique, et de plus est renvoyée à nouveau à partir de la zone de séparation vers la zone de craquage. La durée de l'exposition dans la zone de craquage dans une seule passe peut être courte. Ici la capacité de commande du processus de craquage thermique est élevée, la plage d'ajustement des paramètres de traitement est étendue, le procédé étant assuré de sa polyvalence et de son efficacité.
PCT/RU2007/000433 2007-08-07 2007-08-07 Procédé de craquage thermique de produit d'huile lourde Ceased WO2009022937A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/RU2007/000433 WO2009022937A1 (fr) 2007-08-07 2007-08-07 Procédé de craquage thermique de produit d'huile lourde

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Application Number Priority Date Filing Date Title
PCT/RU2007/000433 WO2009022937A1 (fr) 2007-08-07 2007-08-07 Procédé de craquage thermique de produit d'huile lourde

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2500789C1 (ru) * 2012-12-19 2013-12-10 Андрей Владиславович Курочкин Способ термической конверсии тяжелого углеводородного сырья
RU2536590C1 (ru) * 2013-09-25 2014-12-27 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Установка для термодеструкции нефтяных остатков
RU2536589C1 (ru) * 2013-09-25 2014-12-27 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ фракционирования продуктов термического крекинга
RU2540400C1 (ru) * 2013-10-08 2015-02-10 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ фракционирования продуктов термического крекинга
RU2554005C1 (ru) * 2014-05-23 2015-06-20 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ разделения реакционной смеси продуктов термического крекинга
RU2612963C1 (ru) * 2016-02-24 2017-03-14 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ получения тяжёлого нефтяного топлива
RU2615129C1 (ru) * 2016-06-14 2017-04-04 Андрей Владиславович Курочкин Установка замедленной термической конверсии мазута
RU2626321C1 (ru) * 2016-06-28 2017-07-26 Андрей Владиславович Курочкин Установка замедленной термической конверсии мазута
CN109207196A (zh) * 2018-10-25 2019-01-15 中国石油化工股份有限公司 一种fdfcc催化裂化改质副粗汽油的加工流程
CN110396426A (zh) * 2019-07-26 2019-11-01 南京绿帝环保能源科技有限公司 重油连续式生产燃料油装置
RU2744073C2 (ru) * 2018-01-10 2021-03-02 Андрей Владиславович Курочкин Установка получения мазута замедленной термической конверсией
CN114672344A (zh) * 2022-02-14 2022-06-28 浙江大学杭州国际科创中心 一种重油蒸汽裂解、产物分离回收小试装置及其使用方法
CN116501000A (zh) * 2023-06-26 2023-07-28 深圳市鑫典金光电科技有限公司 一种复合铜散热底板生产设备的控制方法及系统

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6072989A (ja) * 1983-09-30 1985-04-25 Res Assoc Residual Oil Process<Rarop> 重質油の熱分解方法
WO1997019149A1 (fr) * 1995-11-20 1997-05-29 Sergei Vladimirovich Trifonov Installation de craquage thermique de petrole brut
RU2178447C1 (ru) * 2000-08-08 2002-01-20 Горлов Евгений Григорьевич Установка термического крекинга тяжелых нефтяных остатков
RU2246523C1 (ru) * 2003-11-10 2005-02-20 Российский химико-технологический университет им. Д.И. Менделеева Способ углубления термического крекинга тяжелых нефтепродуктов и устройство для его осуществления

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6072989A (ja) * 1983-09-30 1985-04-25 Res Assoc Residual Oil Process<Rarop> 重質油の熱分解方法
WO1997019149A1 (fr) * 1995-11-20 1997-05-29 Sergei Vladimirovich Trifonov Installation de craquage thermique de petrole brut
RU2178447C1 (ru) * 2000-08-08 2002-01-20 Горлов Евгений Григорьевич Установка термического крекинга тяжелых нефтяных остатков
RU2246523C1 (ru) * 2003-11-10 2005-02-20 Российский химико-технологический университет им. Д.И. Менделеева Способ углубления термического крекинга тяжелых нефтепродуктов и устройство для его осуществления

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
DEKHTERMAN A SH: "Oil refining by a fuel variant", KHIMYA, 1988, MOSCOW, pages 52 - 53 *

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2500789C1 (ru) * 2012-12-19 2013-12-10 Андрей Владиславович Курочкин Способ термической конверсии тяжелого углеводородного сырья
RU2536590C1 (ru) * 2013-09-25 2014-12-27 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Установка для термодеструкции нефтяных остатков
RU2536589C1 (ru) * 2013-09-25 2014-12-27 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ фракционирования продуктов термического крекинга
RU2540400C1 (ru) * 2013-10-08 2015-02-10 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ фракционирования продуктов термического крекинга
RU2554005C1 (ru) * 2014-05-23 2015-06-20 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ разделения реакционной смеси продуктов термического крекинга
RU2612963C1 (ru) * 2016-02-24 2017-03-14 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ получения тяжёлого нефтяного топлива
RU2615129C1 (ru) * 2016-06-14 2017-04-04 Андрей Владиславович Курочкин Установка замедленной термической конверсии мазута
RU2626321C1 (ru) * 2016-06-28 2017-07-26 Андрей Владиславович Курочкин Установка замедленной термической конверсии мазута
RU2744073C2 (ru) * 2018-01-10 2021-03-02 Андрей Владиславович Курочкин Установка получения мазута замедленной термической конверсией
CN109207196A (zh) * 2018-10-25 2019-01-15 中国石油化工股份有限公司 一种fdfcc催化裂化改质副粗汽油的加工流程
CN110396426A (zh) * 2019-07-26 2019-11-01 南京绿帝环保能源科技有限公司 重油连续式生产燃料油装置
CN114672344A (zh) * 2022-02-14 2022-06-28 浙江大学杭州国际科创中心 一种重油蒸汽裂解、产物分离回收小试装置及其使用方法
CN114672344B (zh) * 2022-02-14 2023-10-03 浙江大学杭州国际科创中心 一种重油蒸汽裂解、产物分离回收小试装置及其使用方法
CN116501000A (zh) * 2023-06-26 2023-07-28 深圳市鑫典金光电科技有限公司 一种复合铜散热底板生产设备的控制方法及系统
CN116501000B (zh) * 2023-06-26 2023-09-05 深圳市鑫典金光电科技有限公司 一种复合铜散热底板生产设备的控制方法及系统

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