SU854267A3 - Method of catalytic cracking - Google Patents
Method of catalytic cracking Download PDFInfo
- Publication number
- SU854267A3 SU854267A3 SU721780734A SU1780734A SU854267A3 SU 854267 A3 SU854267 A3 SU 854267A3 SU 721780734 A SU721780734 A SU 721780734A SU 1780734 A SU1780734 A SU 1780734A SU 854267 A3 SU854267 A3 SU 854267A3
- Authority
- SU
- USSR - Soviet Union
- Prior art keywords
- catalyst
- riser
- regenerated
- coke
- separation zone
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/321—Catalytic processes
-
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
Description
1one
Изобретение относитс к способам каталитического крекинга углеводородного сырь и может быть использовано в процессе каталитического гидрогенизировани дл получени топливных газов. . The invention relates to methods for the catalytic cracking of hydrocarbon feedstocks and can be used in a catalytic hydrogenation process for the production of fuel gases. .
Известен способ каталитическогй крекинга путем контактировани углеводородного сырь с гор чим регенерированным катализатором в псевдоожиженном слое с, получением продуктов реакции и кокса, адсорбции кокса на катализаторе, который, вывод т на регенерацию, и возврата регенерированного катгшизатора на контактирование The known method of catalytic cracking by contacting the hydrocarbon feedstock with a hot regenerated catalyst in a fluidized bed with obtaining the reaction products and coke, adsorbing coke on the catalyst, which is removed for regeneration, and returning the regenerated catcher to the contacting
Недостатком известного способа вл етс повышенный расход катализатора , что значительно снижает эффективность процесса.The disadvantage of this method is increased catalyst consumption, which significantly reduces the efficiency of the process.
Цель изобретени - интенсификаци процесса каталитического крекинга.The purpose of the invention is to intensify the catalytic cracking process.
Цель достигаетс тем, что в качестве регенерированного катализатора примен ют смесь 25-75 вес.% катализатора , содержащего 0,5-1,0 вес.% примеси кокса.The goal is achieved by using a mixture of 25-75% by weight of catalyst containing 0.5-1.0% by weight of coke impurity as a regenerated catalyst.
На чертеже изображена технологическа схема установки, с помощью которой реализуетс способ.The drawing shows the technological scheme of the installation, with which the method is realized.
Каталитическа установка состоит из вертикального .сто ка 1, располо- . женного над сто ком и соединенногоThe catalytic installation consists of a vertical one. over one hundred and connected
, с ним реактора 2, регенератора 3, трубы 4 подвода регенерированного катализатора, соедин ющей регенератор 3 со сто ком 1, и трубопровода 5 дл циркул ции катализатора, един ющего реактор 2 с нижней частью сто ка 1. Реактор 2 представл ет собой цилиндрическую-.емкость, содержащую псевдоожиженный слой 6 казапизатора и средства 7 и 8 дл отделени углеводородов от вход щего катализатора. Очищенные от катализатора углеводороды отвод тс из реактора 2 по трубопроводу 9. Отделительные средства 7 могут быть выполнены в виде циклона с трубой 10, погруженной в слой 6 катализатора .the reactor 2, the regenerator 3, the pipe 4 for supplying the regenerated catalyst connecting the regenerator 3 to the stand 1, and the pipeline 5 for circulating the catalyst that connects the reactor 2 to the bottom of the stand 1. The reactor 2 is a cylindrical Container containing a fluidized bed 6 of the capsizer and means 7 and 8 for separating the hydrocarbons from the incoming catalyst. The hydrocarbons purified from the catalyst are withdrawn from the reactor 2 via line 9. The separating means 7 can be made in the form of a cyclone with a pipe 10 immersed in the catalyst bed 6.
Циркул ционный трубопровод 5 снабжен золотником 11, который регулирует поток циркулирующего катализатора . На трубопроводе 5 имеетс патрубок 12 дл отгона легких фракций, через который подводитс поток газа. Трубопровод 13 соедин -: ет реактор 2 с регенератором 3 и снабжен золотником 14 дл регулировани потока катализатора из реактора 2 в регенератор 3. Патрубок 15 обеспечивает подвод газа к трубопроводу 13 дл десорбции углеводородов из катализатора, который содержит циклон 16, отдел ющий поступающий в регенератор 3 катализатор от топливного газа, который, в свою очередь , отводитс по трубе 17, Отделенный катализатор возвращаетс IB нижнюю часть регенератора 3 по трубе 18, погруженной в плотный СЛОЙ 19 катализатора. Труба 4 возврта катализатора снабжена золотником 20, регулирующим подачу регенерированного катализатора в сто к, нижн часть которого соединена с патрубком 21 подачи свежего или повторно циркулирующего углеводородного сырь .The circulation pipe 5 is provided with a spool 11, which controls the flow of the circulating catalyst. Pipe 5 has a pipe 12 for stripping the light ends, through which a gas stream is supplied. Pipeline 13 connects -: em reactor 2 to regenerator 3 and is equipped with a spool 14 for controlling the flow of catalyst from reactor 2 to regenerator 3. Pipe 15 provides gas to pipeline 13 to desorb hydrocarbons from the catalyst, which contains a cyclone 16 separating the regenerator 3, the catalyst from the fuel gas, which, in turn, is discharged through the pipe 17, the separated catalyst returns IB the lower part of the regenerator 3 through the pipe 18, immersed in a dense catalyst LAY 19. The catalyst return pipe 4 is provided with a spool 20 that regulates the supply of the regenerated catalyst to one hundred kilograms, the lower part of which is connected to the feed 21 of fresh or recycled hydrocarbon feedstock 21.
Способ каталитического крекинга реализуетс следующим образом.The catalytic cracking method is implemented as follows.
Поступающее сырье выпариваетс , и его пары перевод т катализатор, наход щийс в сто ке 1 в псевдоожиженное состо ние. Лзлее пары вместе с катализатором поступают в реактор 2, проход при этом через слой 6 катализатора. При этом в нижней части сто ка 1 сырье контактирует с регенерированным катешизатором , поступающим из трубопровода 5. Нагретый катализатор выпаривает исходное сырье и вс смесь исходного материала и катализатора проходит через сто к 1 в реактор 2. Из реактора 2 катализатор поступает по трубопроводу 13.в регенератор 3 на регенерацию .The incoming feedstock is evaporated and its vapors convert the catalyst in station 1 to a fluidized state. Lzlee couples with the catalyst enter the reactor 2, while passing through the layer 6 of the catalyst. At the same time, in the lower part of the effluent 1, the feedstock is in contact with the regenerated catechesizer coming from the pipeline 5. The heated catalyst evaporates the feedstock and the entire mixture of the starting material and the catalyst passes through hundred to 1 to the reactor 2. From the reactor 2, the catalyst enters via pipeline 13.c regenerator 3 for regeneration.
В процессе каталитического крекинга углеводород на катализаторе адсорбируетс в виде примеси коксаDuring catalytic cracking, the hydrocarbon on the catalyst is adsorbed as a coke impurity.
с содержанием 0,01-0,4 вес.% и 0,51 ,0 вес.%. Такое содержание кокса на катализаторе находитс , соответственно , в регенераторе и в реакторе , который затем поступает в нижнюю часть сто ка 1 и смешиваетс .with a content of 0.01-0.4 wt.% and 0.51, 0 wt.%. Such a coke content on the catalyst is, respectively, in the regenerator and in the reactor, which then enters the lower part of the effluent 1 and mixes.
Использование в качестве регенерированного катализатора смеси 2575 вес.% катализатора с О,01-0,4 вес.% примесью кокса и 25-75 вес.% ката- лизатора с 0,5-1,0 вес.% примеси кокса позвол ет значительно снизить потери катализатора и улучшить тепловой баланс реакции крекинга, что в целом интенсифицирует процесс крекинга .Using as a regenerated catalyst a mixture of 2575% by weight of catalyst with O, 01-0.4% by weight of coke impurity and 25-75% by weight of catalyst with 0.5-1.0% by weight of coke impurity allows significantly reduce catalyst losses and improve the heat balance of the cracking reaction, which generally intensifies the cracking process.
Claims (1)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13943371A | 1971-05-03 | 1971-05-03 |
Publications (1)
Publication Number | Publication Date |
---|---|
SU854267A3 true SU854267A3 (en) | 1981-08-07 |
Family
ID=22486628
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
SU721780734A SU854267A3 (en) | 1971-05-03 | 1972-05-03 | Method of catalytic cracking |
Country Status (21)
Country | Link |
---|---|
JP (1) | JPS525032B1 (en) |
AR (1) | AR192444A1 (en) |
AU (1) | AU459793B2 (en) |
BE (1) | BE782612A (en) |
BR (1) | BR7202712D0 (en) |
CA (1) | CA967498A (en) |
DD (1) | DD97138A5 (en) |
DE (1) | DE2221618A1 (en) |
DK (1) | DK143988C (en) |
EG (1) | EG10866A (en) |
ES (1) | ES402306A1 (en) |
FI (1) | FI55860C (en) |
FR (1) | FR2135237B1 (en) |
GB (1) | GB1387127A (en) |
HU (1) | HU166038B (en) |
IT (1) | IT957690B (en) |
NL (1) | NL173482C (en) |
SE (1) | SE396087B (en) |
SU (1) | SU854267A3 (en) |
TR (1) | TR17454A (en) |
ZA (1) | ZA722959B (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2013142014A1 (en) * | 2012-03-20 | 2013-09-26 | Uop Llc | Process and apparatus for mixing two streams of catalyst |
RU2510966C2 (en) * | 2008-09-30 | 2014-04-10 | Юоп Ллк | Device and method for mixing the recovered catalyst with carbonised catalyst |
US8815166B2 (en) | 2012-03-20 | 2014-08-26 | Uop Llc | Process and apparatus for mixing two streams of catalyst |
RU2575934C1 (en) * | 2011-12-12 | 2016-02-27 | Юоп Ллк | Method and apparatus for mixing two catalyst streams |
RU2576323C1 (en) * | 2011-12-12 | 2016-02-27 | Юоп Ллк | Method and device for mixing two flows of catalyst |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2377935A (en) * | 1941-04-24 | 1945-06-12 | Standard Oil Co | Catalytic hydrocarbon conversion system |
-
1972
- 1972-04-25 BE BE782612A patent/BE782612A/en unknown
- 1972-05-02 FI FI1238/72A patent/FI55860C/en active
- 1972-05-02 DK DK218172A patent/DK143988C/en active
- 1972-05-02 SE SE7205775A patent/SE396087B/en unknown
- 1972-05-02 ES ES402306A patent/ES402306A1/en not_active Expired
- 1972-05-02 HU HUUI191A patent/HU166038B/hu unknown
- 1972-05-02 EG EG181/72A patent/EG10866A/en active
- 1972-05-02 ZA ZA722959A patent/ZA722959B/en unknown
- 1972-05-02 GB GB2034072A patent/GB1387127A/en not_active Expired
- 1972-05-02 IT IT4999972A patent/IT957690B/en active
- 1972-05-02 BR BR2712/72A patent/BR7202712D0/en unknown
- 1972-05-02 CA CA141,084A patent/CA967498A/en not_active Expired
- 1972-05-03 AU AU41834/72A patent/AU459793B2/en not_active Expired
- 1972-05-03 SU SU721780734A patent/SU854267A3/en active
- 1972-05-03 FR FR7215630A patent/FR2135237B1/fr not_active Expired
- 1972-05-03 DE DE19722221618 patent/DE2221618A1/en active Pending
- 1972-05-03 TR TR17454A patent/TR17454A/en unknown
- 1972-05-03 DD DD162719A patent/DD97138A5/xx unknown
- 1972-05-03 AR AR241776A patent/AR192444A1/en active
- 1972-05-03 NL NLAANVRAGE7205939,A patent/NL173482C/en not_active IP Right Cessation
- 1972-05-04 JP JP47044518A patent/JPS525032B1/ja active Pending
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2510966C2 (en) * | 2008-09-30 | 2014-04-10 | Юоп Ллк | Device and method for mixing the recovered catalyst with carbonised catalyst |
RU2575934C1 (en) * | 2011-12-12 | 2016-02-27 | Юоп Ллк | Method and apparatus for mixing two catalyst streams |
RU2576323C1 (en) * | 2011-12-12 | 2016-02-27 | Юоп Ллк | Method and device for mixing two flows of catalyst |
WO2013142014A1 (en) * | 2012-03-20 | 2013-09-26 | Uop Llc | Process and apparatus for mixing two streams of catalyst |
US8815166B2 (en) | 2012-03-20 | 2014-08-26 | Uop Llc | Process and apparatus for mixing two streams of catalyst |
US8936758B2 (en) | 2012-03-20 | 2015-01-20 | Uop Llc | Process and apparatus for mixing two streams of catalyst |
RU2571119C1 (en) * | 2012-03-20 | 2015-12-20 | Юоп Ллк | Method and device for mixing two catalyst flows |
Also Published As
Publication number | Publication date |
---|---|
BR7202712D0 (en) | 1973-06-21 |
DD97138A5 (en) | 1973-04-20 |
SE396087B (en) | 1977-09-05 |
NL7205939A (en) | 1972-11-07 |
FR2135237A1 (en) | 1972-12-15 |
EG10866A (en) | 1976-08-31 |
AU4183472A (en) | 1973-11-08 |
ES402306A1 (en) | 1975-04-01 |
DE2221618A1 (en) | 1972-11-23 |
ZA722959B (en) | 1973-02-28 |
IT957690B (en) | 1973-10-20 |
HU166038B (en) | 1974-12-28 |
NL173482B (en) | 1983-09-01 |
JPS525032B1 (en) | 1977-02-09 |
FI55860C (en) | 1979-10-10 |
GB1387127A (en) | 1975-03-12 |
NL173482C (en) | 1984-02-01 |
CA967498A (en) | 1975-05-13 |
AU459793B2 (en) | 1975-04-10 |
BE782612A (en) | 1972-10-25 |
TR17454A (en) | 1975-07-23 |
FR2135237B1 (en) | 1975-08-29 |
DK143988B (en) | 1981-11-09 |
AR192444A1 (en) | 1973-02-21 |
FI55860B (en) | 1979-06-29 |
DK143988C (en) | 1982-05-03 |
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