US3725495A - Catalytic steam cracking of hydrocarbons and catalysts therefor - Google Patents

Catalytic steam cracking of hydrocarbons and catalysts therefor Download PDF

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Publication number
US3725495A
US3725495A US00099271A US3725495DA US3725495A US 3725495 A US3725495 A US 3725495A US 00099271 A US00099271 A US 00099271A US 3725495D A US3725495D A US 3725495DA US 3725495 A US3725495 A US 3725495A
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process according
steam
feedstock
reactor
added
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US00099271A
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English (en)
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J Wrisberg
K Andersen
E Mogensen
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Fluor Corp
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Fluor Corp
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—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
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
    • C07C2521/04—Alumina
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
    • C07C2523/04—Alkali metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/24—Chromium, molybdenum or tungsten
    • C07C2523/26—Chromium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/32—Manganese, technetium or rhenium
    • C07C2523/34—Manganese
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
    • C07C2523/74—Iron group metals
    • C07C2523/745—Iron
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00—Chemistry of hydrocarbon compounds
    • Y10S585/949—Miscellaneous considerations
    • Y10S585/95—Prevention or removal of corrosion or solid deposits

Definitions

  • a typical steam cracker produces methane and hydrogen 18 percent, ethylene 32 percent, ethane 5 percent, propylene 18 percent, butadiene 5 percent, butylene 4 percent, and gasoline/fuel oil 18 percent (percent by weight of feed).
  • catalyst compositions for steam cracking of hydrocarbons have been proposed. These compositions include combinations of zirconium oxide and one or more of a number of other oxides among which are oxides of the rare earth metals, antimony oxide, and inacv vtive oxides rich in magnesium oxide. Further oxides which might optionally be included in the catalyst composition in small amounts are iron oxide, aluminum ox ide, copper oxide, calcium oxide, barium oxide, silicium oxide, and titanium oxide. These catalysts are claimed to operate without carbon deposition at rather low space velocities.
  • butadiene, and aromatics from saturated hydrocarbons which gives improved yield and thermal efficiencies while being capable of operating at high space velocity without significant carbon deposition on the catalyst.
  • a process for the manufacture of unsaturated hydrocarbons by a gaseous catalytic reaction wherein a feedstock substantially comprising saturated hydrocarbons is contacted at a temperature below l,000C and a pressure of 0.1-50 atm.abs. in the presence of added steam with a catalyst comprising a major proportion of at least one oxide of zirconium or hafnium together with at least 5 percent of active aluminum oxide as well as at least 5 percent of at least one oxide of manganese, chromium or iron, and a small amount not exceeding l0 -percentof at least one compound of an alkali metal or alkaline earth metal.
  • a catalyst for the manufacture of unsaturated hydrocarbons from saturated hydrocarbons in the presence of steam comprising a major proportion of at least one oxide of zirconium or hafnium, together with at least 5 percent of active aluminum oxide, as well as at least 5 percent of one oxide of manganese, chromium, or iron, and a small amount not exceeding 10 percent of at least one compound of an alkali metal or alkalineearth metal.
  • the process is carried out at a temperature in the range 200"900"C, preferably in the range 500 850'C. it is also preferred to use pressures in the range 1-15 atm.abs. measured at the reactor outlet.
  • the major component of the catalyst used in the A process according to the present invention is zirconium or hafnium oxide or both. This component should be present in an amount of at least 50 wt.% up to It should be noted that a catalyst substantially consisting of, for example, zirconium oxide is not very'practicable because such a catalyst does not possess adequate mechanical strength unless it is subjected to a heat treatment at high temperatures such as temperatures above l,000C. It has been found that the presence of active aluminum oxide in the catalyst composition facilitates its preparation so that a satisfactory strength can be obtained from a heat treatment at a temperature below l,000C.
  • the reactive aluminum oxide is added during the preparation of the catalyst either as such or as a compound which on heating transforms into an active aluminum oxide such as for example precipitated aluminum hydroxide.
  • the amount of active aluminum oxide is not very critical and an amount of at least 5 wt.% is satisfactory.
  • the catalyst may contain up to 30 wt.% of active alumina, 10 wt.% being the preferred level.
  • the catalyst used in the process accord ing to the present invention contains at least 5 wt.% up to about 40 wt.% of one or more of the oxides of manganese, chromium, or iron together with an alkali metal compound or an alkaline earth metal compound or both in a total amount of 0.1 to 10' wt.% calculated in the oxide. If an alkaline earth compound is present it ispreferred to have a compound of an alkali metal present also.
  • the use of a potassium compound in an amount of 0.3 to 7 wt.% calculated as the oxide is especially preferred.
  • Suitable saturated hydrocarbons include methane, ethane, propane, butane as well as liquid hydrocarbons such as light naphtha and even crude oil.
  • Our process and catalyst readily tolerate the presence of sulphur which is even desirable since it can passivate the free metal surfaces in the reactor. The sulphur may -made on the equipment are accordingly reduced,
  • the dried precipitate was mixed with 37 g graphite and 28 g cellulose fiber and ground for 6 hours in a ball mill, after which the mixture was tabletted. The tablets were then calcined for 2 hours at 850C.
  • the resulting catalyst A had the following composition (percentages by weight):
  • the resulting catalyst 13 had the following composition (by weight) 13% Al O 52% ZrO 27% MnO 8% K 0.
  • the naphtha-water feed was first passed through a preheater and then through the reactor, the space velocity being 4.2 liq. vol./vol. catalyst/h.
  • the feed passed downwards through the reactor, the temperature at the top of the catalyst bed being 590C and the tempera ture at the center and at the bottom of the bed being 750C.
  • the reactor effluent was quenched by water injection in the reactor outlet and the composition of the effluent product gas determined on a gas-chromatograph. The results of these investigations are shown in the accompanying table I.
  • Catalysts A, B, C, and D which are in accordance with the present invention, all gave an almost complete conversion of the hydrocarbon feed with about 1 percent or less unconverted hydrocarbon feed in the product.
  • Catalyst E which is not in accordance with the present invention, gave a complete conversion right from the start, however, there was a gradual increase in unconverted hydrocarbon feed in the product, and after hours operation 20 percent of the hydrocarbon feed passed the catalyst almost unchanged.
  • catalyst F which is in accordance with the present invention, the conversion was incomplete from the start, however, after a few hours operation the conversion became complete and during the remaining part of the experiment the amount of unconverted hydrocarbon feed in the product was insignificant.
  • catalyst B was tested in a pilot plant reactor (Reactor Two) having a height of 6 m and an internal diameter of 0.09 m. A series of oilfired burners were provided to heat the reactor. To this reactor was fed a feed of 200 kg/h of naphtha of the same composition as before, together with 120 kg/h steam (i.e., a steam-naphtha ratio of 0.6).
  • the inlet pressure was 7 kg/cm
  • the outlet pressure 0.3 kg/cm
  • the heat flux at the inner reactor wall was 80,000 Kcal/mlf
  • Table II The results of investigations using 36 l of catalyst B in this reactor are shown in table II. Although a very high space velocity of 8.6 liq.vol./v0l.catalyst/h was used in this experiment only insignificant amounts of unconverted hydrocarbon feed appeared in the product, the liquid product consisting mainly of aromatics.
  • reaction is carried out at a temperature in the range 3.
  • reaction is carried out at a pressure of latm.abs. measuredat the reactor outlet. 7
  • the feedstock consists entirely of a saturated hydrocarbon or a mixture of saturated hydrocarbons.
  • a process for the manufacture of unsaturated hydrocarbons by a gaseous catalytic reaction wherein a feedstock substantially comprising saturated hydrocarbons is contacted at a temperature in the range 500850C and a pressure in the range l-15 atm.abs. measured at the reactor outlet in the presence of added steam with a catalyst comprising 50-80 wt.% zirconium and/or hafnium oxide, together with 5-30 wt.% active alumina,- as well as 5-40 wt.% of at least one oxide of chromium manganese and/or iron 'and 0.3-7.0 wt.% of at least one compound of an alkali metal and/or alkaline earth metal.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
US00099271A 1969-12-23 1970-12-17 Catalytic steam cracking of hydrocarbons and catalysts therefor Expired - Lifetime US3725495A (en)

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Application Number Priority Date Filing Date Title
GB6255269 1969-12-23

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Country Status (9)

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US (1) US3725495A (fr)
CA (1) CA973152A (fr)
DE (1) DE2063172A1 (fr)
DK (1) DK139907B (fr)
ES (1) ES386738A1 (fr)
FR (1) FR2072015B1 (fr)
GB (1) GB1306087A (fr)
NL (1) NL7018312A (fr)
ZA (1) ZA708259B (fr)

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3948755A (en) * 1974-05-31 1976-04-06 Standard Oil Company Process for recovering and upgrading hydrocarbons from oil shale and tar sands
US3948754A (en) * 1974-05-31 1976-04-06 Standard Oil Company Process for recovering and upgrading hydrocarbons from oil shale and tar sands
US3985641A (en) * 1974-04-15 1976-10-12 Phillips Petroleum Company Catalytic cracking of alkanes
DE2640278A1 (de) * 1975-09-25 1977-03-31 British Petroleum Co Verfahren zur herstellung von olefinen
US4093536A (en) * 1974-04-15 1978-06-06 Phillips Petroleum Company Catalytic cracking and dehydrocyclizing of alkanes using alkaline earth oxides promoted with manganese oxide and/or rhenium oxide
US4111793A (en) * 1975-09-25 1978-09-05 The British Petroleum Company Limited Olefins production
US4385193A (en) * 1980-06-06 1983-05-24 Shell Oil Company Process for the preparation of middle distillates
FR2525583A1 (fr) * 1982-04-26 1983-10-28 United Technologies Corp Installation et procede de reformage a la vapeur avec catalyseur a activite elevee
US5093540A (en) * 1990-08-31 1992-03-03 Shell Oil Company Process for selectively converting linear paraffins to linear alpha olefins
US20030232720A1 (en) * 2002-06-12 2003-12-18 Saeed Alerasool Paraffin dehydrogenation catalyst
US20070293714A1 (en) * 2004-03-31 2007-12-20 Jun Long Zeolite-Containing Hydrocarbon-Converting Catalyst, the Preparation Process Thereof, and a Process for Converting Hydrocarbon Oils with the Catalyst
WO2008028343A1 (fr) 2006-08-31 2008-03-13 China Petroleum & Chemical Corporation Procédé de conversion catalytique d'hydrocarbures
WO2008034299A1 (fr) 2006-08-31 2008-03-27 China Petroleum & Chemical Corporation Catalyseur de conversion d'hydrocarbures
US20090012340A1 (en) * 2007-07-05 2009-01-08 Lg Chem, Ltd. Thermal-cracking method of hydrocarbon
US20090105066A1 (en) * 2007-05-25 2009-04-23 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US20090234167A1 (en) * 2008-03-14 2009-09-17 Catalytic Distillation Technologies Process for converting methane to ethylene
US20100133146A1 (en) * 2008-12-02 2010-06-03 Van Egmond Cor Franciscus Coil for pyrolysis heater and method of cracking
US20100270210A1 (en) * 2007-06-27 2010-10-28 Jun Long Catalytic cracking catalyst, its preparation and use
US20100312035A1 (en) * 2009-06-05 2010-12-09 Basf Catalysts Llc Alkane dehydrogenation catalysts
US8674158B2 (en) * 2009-06-08 2014-03-18 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
CN109232153A (zh) * 2018-09-27 2019-01-18 江苏博颂化工科技有限公司 一种石脑油制备低碳烯烃的方法
WO2020063449A1 (fr) * 2018-09-27 2020-04-02 上海卓然工程技术股份有限公司 Catalyseur de craquage catalytique de naphta, procédé de craquage catalytique et dispositif de réaction
US11225612B2 (en) 2020-03-27 2022-01-18 Saudi Arabian Oil Company Catalyst and process for catalytic steam cracking of heavy distillate
US11866397B1 (en) 2023-03-14 2024-01-09 Saudi Arabian Oil Company Process configurations for enhancing light olefin selectivity by steam catalytic cracking of heavy feedstock

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4620052A (en) * 1985-07-25 1986-10-28 Phillips Petroleum Company Dehydrogenation and cracking of C3 and C4 hydrocarbons
US4579997A (en) * 1985-07-25 1986-04-01 Phillips Petroleum Company Olefin production over catalytic oxides of Mn and at least one of Nb and a lanthanide
US4620051A (en) * 1985-07-25 1986-10-28 Philips Petroleum Company Dehydrogenation and cracking of C3 and C4 hydrocarbons to less saturated hydrocarbons
US4658081A (en) * 1985-07-25 1987-04-14 Phillips Petroleum Company Propylene and ethylene selectivity with H2 S
US4621162A (en) * 1985-07-25 1986-11-04 Phillips Petroleum Company Method for conversion of C3 and C4 hydrocarbons to olefinic products
US4621163A (en) * 1985-07-25 1986-11-04 Phillips Petroleum Company Conversion of C3 and C4 hydrocarbons to less saturated hydrocarbons
US4613722A (en) * 1985-07-25 1986-09-23 Phillips Petroleum Company Dehydrogenation of C3 and C4 hydrocarbons over an iron-based catalyst

Citations (6)

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US2392750A (en) * 1942-08-22 1946-01-08 Standard Oil Dev Co Dehydrogenation of hydrocarbons
US2754354A (en) * 1952-08-18 1956-07-10 Price Carl Insulator
US2894046A (en) * 1957-04-12 1959-07-07 Universal Oil Prod Co Manufacture of para-xylene
US2941016A (en) * 1957-11-05 1960-06-14 Hoechst Ag Process for preparing aromatic hydrocarbons
US3179602A (en) * 1961-09-06 1965-04-20 Monsanto Co Preparation of a chromia-alumina hydrocarbon conversion catalyst
US3624176A (en) * 1968-06-25 1971-11-30 Azote & Prod Chim Catalytic process for producing gas mixtures having high ethylene contents

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NL6905469A (fr) * 1968-04-09 1969-10-13
FR1603019A (fr) * 1968-05-30 1971-03-15

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2392750A (en) * 1942-08-22 1946-01-08 Standard Oil Dev Co Dehydrogenation of hydrocarbons
US2754354A (en) * 1952-08-18 1956-07-10 Price Carl Insulator
US2894046A (en) * 1957-04-12 1959-07-07 Universal Oil Prod Co Manufacture of para-xylene
US2941016A (en) * 1957-11-05 1960-06-14 Hoechst Ag Process for preparing aromatic hydrocarbons
US3179602A (en) * 1961-09-06 1965-04-20 Monsanto Co Preparation of a chromia-alumina hydrocarbon conversion catalyst
US3624176A (en) * 1968-06-25 1971-11-30 Azote & Prod Chim Catalytic process for producing gas mixtures having high ethylene contents

Cited By (47)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3985641A (en) * 1974-04-15 1976-10-12 Phillips Petroleum Company Catalytic cracking of alkanes
US4093536A (en) * 1974-04-15 1978-06-06 Phillips Petroleum Company Catalytic cracking and dehydrocyclizing of alkanes using alkaline earth oxides promoted with manganese oxide and/or rhenium oxide
US3948755A (en) * 1974-05-31 1976-04-06 Standard Oil Company Process for recovering and upgrading hydrocarbons from oil shale and tar sands
US3948754A (en) * 1974-05-31 1976-04-06 Standard Oil Company Process for recovering and upgrading hydrocarbons from oil shale and tar sands
DE2640278A1 (de) * 1975-09-25 1977-03-31 British Petroleum Co Verfahren zur herstellung von olefinen
US4087350A (en) * 1975-09-25 1978-05-02 The British Petroleum Company Limited Olefins production by steam cracking over manganese catalyst
US4111793A (en) * 1975-09-25 1978-09-05 The British Petroleum Company Limited Olefins production
US4385193A (en) * 1980-06-06 1983-05-24 Shell Oil Company Process for the preparation of middle distillates
FR2525583A1 (fr) * 1982-04-26 1983-10-28 United Technologies Corp Installation et procede de reformage a la vapeur avec catalyseur a activite elevee
US4451578A (en) * 1982-04-26 1984-05-29 United Technologies Corporation Iron oxide catalyst for steam reforming
US5093540A (en) * 1990-08-31 1992-03-03 Shell Oil Company Process for selectively converting linear paraffins to linear alpha olefins
US20030232720A1 (en) * 2002-06-12 2003-12-18 Saeed Alerasool Paraffin dehydrogenation catalyst
US7012038B2 (en) * 2002-06-12 2006-03-14 Engelhard Corporation Paraffin dehydrogenation catalyst
US20070293714A1 (en) * 2004-03-31 2007-12-20 Jun Long Zeolite-Containing Hydrocarbon-Converting Catalyst, the Preparation Process Thereof, and a Process for Converting Hydrocarbon Oils with the Catalyst
US7923399B2 (en) 2004-03-31 2011-04-12 China Petroleum & Chemical Corporation Zeolite-containing hydrocarbon-converting catalyst, the preparation process thereof, and a process for converting hydrocarbon oils with the catalyst
WO2008028343A1 (fr) 2006-08-31 2008-03-13 China Petroleum & Chemical Corporation Procédé de conversion catalytique d'hydrocarbures
WO2008034299A1 (fr) 2006-08-31 2008-03-27 China Petroleum & Chemical Corporation Catalyseur de conversion d'hydrocarbures
US8900445B2 (en) 2006-08-31 2014-12-02 China Petroleum & Chemical Corporation Process for the catalytic conversion of hydrocarbons
US8716163B2 (en) 2006-08-31 2014-05-06 China Petroleum & Chemical Corporation Hydrocarbon conversion catalyst
US20090264693A1 (en) * 2006-08-31 2009-10-22 China Petroleum & Chemical Corporation Process for the catalytic conversion of hydrocarbons
US20090325786A1 (en) * 2006-08-31 2009-12-31 China Petroleum & Chemical Corporation Hydrocarbon conversion catalyst
US8492305B2 (en) * 2007-05-25 2013-07-23 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US8123931B2 (en) * 2007-05-25 2012-02-28 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US20090105066A1 (en) * 2007-05-25 2009-04-23 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US8569200B2 (en) * 2007-05-25 2013-10-29 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US20120108417A1 (en) * 2007-05-25 2012-05-03 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US20120108416A1 (en) * 2007-05-25 2012-05-03 Lg Chem, Ltd. Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same
US9486795B2 (en) 2007-06-27 2016-11-08 China Petroleum & Chemical Corporation Catalytic cracking catalyst, its preparation and use
US20100270210A1 (en) * 2007-06-27 2010-10-28 Jun Long Catalytic cracking catalyst, its preparation and use
US20090012340A1 (en) * 2007-07-05 2009-01-08 Lg Chem, Ltd. Thermal-cracking method of hydrocarbon
US7951987B2 (en) 2007-07-05 2011-05-31 Lg Chem, Ltd. Thermal-cracking method of hydrocarbon
CN101353590B (zh) * 2007-07-05 2012-07-25 Lg化学株式会社 烃的热裂解方法
US8471082B2 (en) * 2008-03-14 2013-06-25 Catalytic Distillation Technologies Process for converting methane to ethylene
US20090234167A1 (en) * 2008-03-14 2009-09-17 Catalytic Distillation Technologies Process for converting methane to ethylene
US8163170B2 (en) * 2008-12-02 2012-04-24 Lummus Technology Inc. Coil for pyrolysis heater and method of cracking
US20100133146A1 (en) * 2008-12-02 2010-06-03 Van Egmond Cor Franciscus Coil for pyrolysis heater and method of cracking
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GB1306087A (fr) 1973-02-07
DE2063172A1 (de) 1971-07-01
DK139907C (fr) 1979-10-08
FR2072015A1 (fr) 1971-09-24
NL7018312A (fr) 1971-06-25
FR2072015B1 (fr) 1975-01-10
ES386738A1 (es) 1974-02-01
ZA708259B (en) 1971-08-25
CA973152A (en) 1975-08-19
DK139907B (da) 1979-05-14

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