WO2001047842A1 - Process for the production of olefins - Google Patents
Process for the production of olefins Download PDFInfo
- Publication number
- WO2001047842A1 WO2001047842A1 PCT/GB2000/004794 GB0004794W WO0147842A1 WO 2001047842 A1 WO2001047842 A1 WO 2001047842A1 GB 0004794 W GB0004794 W GB 0004794W WO 0147842 A1 WO0147842 A1 WO 0147842A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- metal
- catalyst
- platinum
- group
- hydrocarbon
- 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
- C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
- C07C5/48—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
-
- 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
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36
- C07C2523/56—Platinum group metals
- C07C2523/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
-
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a process for the production of olefins.
- Olefins such as ethylene and propylene may be produced by a variety of processes, including the steam cracking of hydrocarbons or by the dehydrogenation of paraffinic feedstocks. More recently, olefins have been produced by a process known as auto-thermal cracking. In such a process, a hydrocarbon feed is mixed with an oxygen- containing gas and contacted with a catalyst. The hydrocarbon feed is partially combusted, and the heat produced is used to drive the dehydrogenation reaction.
- Preferred catalysts are supported platinum catalysts such as platinum/gamma alumina spheres, and platinum/monoliths such as platinum/cordierite or mullite monoliths.
- platinum catalysts are modified with tin, copper or antimony. Specifically, Pt/Sn, Pt/Cu, Pt/Sb and Pt/Sn/Sb catalysts are disclosed.
- the present invention provides a process for the production of an olefin from a hydrocarbon, which process comprises: partially combusting the hydrocarbon and an oxygen-containing gas in the presence of a catalyst, characterised in that the catalyst comprises platinum and at least one further metal, said further metal being a Group IIIA, Group IVA, VA or a transition metal; wherein said catalyst is a) not a platinum catalyst consisting essentially of platinum modified with Sn, Cu or mixtures thereof, and b) not a platinum catalyst consisting essentially of platinum modified with Sb or a mixture of Sb and Sn
- the term "further metal” covers all elements of Group IIIA, IVA, NA and the transition metal series of the Periodic Table
- the platinum and at least one further metal may be present in the catalyst in any form, for example, in metallic form, or in the form of a metal compound, such as an oxide
- the partial combustion reaction is carried out by contacting a feed comprising the hydrocarbon and a molecular oxygen containing gas with the catalyst Any suitable oxygen-containing gas may be employed, oxygen being preferred
- the preferred stoichiometric ratio of hydrocarbon to oxygen is 5 to 16, preferably, 5 to 13 5 times, more preferably, 6 to 10 times the stoichiometric ratio of hydrocarbon to oxygen required for complete combustion of the hydrocarbon to carbon dioxide and water
- hydrogen is co-fed into the reaction It is believed that in the presence of the catalyst, hydrogen combusts preferentially relative to the hydrocarbon, thereby increasing the olefin selectivity of the overall process
- Additional feed components such as nitrogen, carbon monoxide and steam may also be fed into the reaction.
- Suitable Group IIIA metals include Al, Ga, In and Tl Of these, Ga and In are preferred Suitable Group IVA metals include Ge, and Pb Of these, Ge is preferred
- Suitable Group VA metals include Bi
- Suitable metals in the transition metal series are any metal from Group IB to VIIIB of the Periodic Table
- transition metals selected from Groups IB, DOB, VTB, VIIB and VIIIB of the Periodic Table are preferred Examples of such metals include Cr, Mo, W, Fe, Ru, Os, Co, Rh, Ir, ⁇ i, Pd, Ag, Au, Zn, Cd and Hg
- Preferred transition metals are Mo, Rh, Ru, Ir, Pd, and Zn
- the catalyst comprises only one metal selected from Group IIIA, Group IVA, VA and the transition metal series.
- the catalyst may comprise Pt and one of Ga, In, Ge and Bi.
- platinum may nominally form between 0.01 and 5.0 wt %, preferably, between 0.01 and 2.0 wt %, and more preferably, between 0.05 and 1.0 wt % of the total weight of the catalyst. It should be noted, however, that not all the metal employed during the preparation of the catalyst necessarily becomes incorporated in the catalyst composition. Thus, the actual loading of metal may differ from the nominal loading. To ensure that the desired actual metal concentrations are achieved, the nominal metal concentrations may have to be varied accordingly.
- the actual loading of platinum may be between 10 and up to 100% of the nominal loading. Preferably, the actual loadings are above 40%, more preferably, above 70 % (eg 90 to 99%o) of the nominal values.
- platinum may actually form between 0.01 and 5.0 wt %, preferably, between 0.01 and 2.0 wt %, and more preferably, between 0.05 and 1.0 wt %> of the total weight of the catalyst.
- the atomic ratio of platinum to the Group IIIA, IVA or transition metal may be 1 : 0.1 - 50.
- Pt:Ga Preferred atomic ratios of Pt:Ga are 1 :0.1 - 20.0, more preferably, 1 : 0.2 - 15.0, even more preferably, 1 : 1.0 - 8.0, most preferably, 1 :5.0 - 8.0, for example, 1 :7.5.
- Preferred atomic ratios of Pt:In are 1 :0.1 - 10.0, more preferably, 1 : 0.2 - 7.0, and most preferably, 1 :0.8 - 3.0., for example, 1 : 1.3.
- Preferred atomic ratios ofPt:Ge are 1 : 0.1 - 20.0, more preferably, 1 : 0.2 - 15.0 and most preferably, 1 :0.5 - 12, for example, 1 : 10.8.
- Pt:Bi are 1 : 0.1 - 20.0, more preferably, 1 : 0.2 - 15.0 and most preferably, 1 :0.5 - 10.0.
- the metal is preferably Mo, Rh, Ru, Ir or Zn.
- the catalyst comprises at least two metals selected from Group IIIA, Group IVA, VA and the transition metal series.
- the catalyst may comprise Pt, Pd and Sn or Pt, Pd and Cu. Platinum may nominally form between
- the actual loading of metal may differ from the nominal loading
- the actual loading of platinum may be between 10 and up to 100%> of the nominal value
- the actual loadings are above 40%>, more preferably, above 70 % (eg 90 - 99%) of the nominal values
- the actual loading of platinum is between 0 01 and 5 wt %, preferably, between 0 01 and 2 0 wt %, and more preferably, 0 05 - 1 0 wt % of the total weight of the catalyst
- the catalyst comprises a) platinum, b) a further transition metal and c) a Group IIIA or IVA metal
- the transition metal b) is preferably palladium
- the metal c) is, preferably, a Group IVA metal, more preferably Sn or Ge
- the atomic ratio of metal b) (eg palladium) to platinum may be 1 0 1 - 10 0, preferably, 1 0 5 - 8 0, and more preferably, 1 1 0 -5 0
- the atomic ratio of metal b) (eg palladium) to metal c) (eg Sn or Cu) may be 1 0 1 - 60, preferably, 1 0 1 - 50, for example, 1 0 1 - 12 Where metal b) is Pd and metal c) is Sn, the Pd Sn atomic ratio is preferably 1 0 1 - 60, more preferably, 1 0 1 - 50, for example, 1 0 1 -12 0 Where metal b) is Pd, and
- the catalyst employed may be unsupported
- the catalyst may be in the form of a metal gauze
- the catalyst employed in the present process is a supported catalyst
- the catalyst may be supported on any suitable support Ceramic supports are generally preferred, although metal supports may also be employed Where ceramic supports are used, the composition of the ceramic support may be any oxide or combination of oxides that is stable at high temperatures of, for example, 600°C and 1200°C
- the support material preferably has a low thermal expansion coefficient, and is resistant to phase separation at high temperatures Suitable ceramic supports include lithium aluminium silicate (LAS), alumina ( ⁇ -
- the supports may be wash-coated, for example, with ⁇ - Al O 3
- the structure of the support material is important, as this may affect flow patterns through the catalyst Such flow patterns may influence the transport of reactants and products to and from the catalyst surface, thereby affecting the catalyst's activity
- the substrate is a continuous multi-channel ceramic structure, such as a foam, a regular channelled monolith or a fibrous pad
- foam monolith structures tend to provide tortuous paths for reactants and products
- Such supports may have 20 to 80, preferably, 30 to 50 pores per inch Channel monoliths generally have straighter, channel-like pores These pores are generally smaller, and there may be 80 or more pores per linear inch of catalyst
- the support may be in the form of spheres or other granular shapes, or may be present as a thin layer or wash coat on another substrate
- the catalyst employed in the present invention may comprise further elements, such as alkali metals Suitable alkali metals include lithium, sodium, potassium and caesium
- the catalyst employed in the present invention may be prepared by any method known in the art For example, gel methods and wet-impregnation techniques may be employed Typically, the support is impregnated with one or more solutions comprising the metals, dried and then calcined in air The support may be impregnated in one or more steps Preferably, multiple impregnation steps are employed The support is preferably dried and calcined between each impregnation, and then subjected to a final calcination, preferably, in air The calcined support may then be reduced, for example, by heat treatment in a hydrogen atmosphere
- the support material is preferably impregnated in a platinum palladium solution, and then in a solution comprising tin
- the catalyst is dried at eg 50 to 200°C, and calcined at eg 100 to 700°C e g 300 to 700°C,between each impregnation
- the support is then subjected to a final calcination step at eg 400 to 1500°C in air
- the catalyst may then be reduced in, for example, a hydrogen atmosphere This reduction step may be carried out at temperatures of up to 1000°C, for example, 300 to 750 °C are employed
- the catalyst may be in the form of a fluidised or fixed bed Preferably, a fixed bed catalyst is employed
- the partial combustion reaction may be suitably carried out at a catalyst exit temperature of between 600°C and 1200°C, preferably between 850°C and 1050°C and most preferably, between 900°C and 1000°C
- the reaction may be carried out at atmospheric or elevated pressure Suitable pressures range from 0 to 2 bara, preferably 1 5 to 2 bara, for example 1 8 bara Elevated pressures of for example, 2 to 50 bara, may also be suitable
- the hydrocarbon may comprise any suitable hydrocarbon
- gaseous hydrocarbons are employed Suitable gaseous hydrocarbons include ethane, propane, butane and mixtures thereof
- the hydrocarbon is passed over the catalyst at a gas hourly space velocity of greater than 10,000 h "1 , preferably above 20,000 h "1 and most preferably, greater than 100,000 h _1 It will be understood, however, that the optimum gas hourly space time velocity will depend upon the pressure and nature of the feed composition
- heat may also be supplied by pre-heating the hydrocarbon
- the temperature to which the hydrocarbon, oxygen-containing gas and (optionally) hydrogen mixture may be preheated is limited by the autoignition properties (eg temperature) of the feed
- reaction products may be quenched as they emerge from the reaction chamber to avoid further reactions taking place
- Any coke produced in the process of the present invention may be removed by mechanical means, or using one of the decoking methods described in EP 0 709 446
- Figure 1 depicts an apparatus 10 comprising a reactor 12 surrounded by a furnace 14
- the reactor 12 may be formed of quartz or metal Where a metal reactor 12 is employed, the inside of the reactor is lined with quartz (not shown)
- quartz not shown
- metal reactors are more susceptible to heat loss than quartz reactors
- the reactor 12 is coupled to an oxygen supply 16 and a hydrocarbon feed supply 18
- the hydrocarbon feed comprises ethane, and hydrogen and nitrogen
- a catalyst 20 is located within the reactor 12
- the catalyst 20 is positioned between a pair of LAS heat shields 22, 24
- the furnace is set to minimise heat losses, and the reactants 16, 18 are introduced into the reactor via line 26 As the reactants contact the catalyst 20, some of the ethane in the hydrocarbon feed 18 combusts to produce water and carbon oxides
- the hydrogen co-feed also combusts to produce water Both these combustion reactions are exothermic, and the heat produced is used to drive the dehydrogenation of ethane to ethylene Examples
- the catalyst was prepared by multiple impregnation of a lithium aluminium silicate support having a high purity alumina (HP A) wash-coat.
- the support was impregnated in 1) a platinum/palladium solution ((NH 3 ) 4 Pt ⁇ Cl 2 , (NH 3 ) 4 Pd ⁇ Cl 2 ), and 2) an
- the catalyst was analysed and found to have 0.36 wt % Pt, 0.04 wt % Pd and
- a catalyst having a nominal loading of 1 wt % Pt was prepared by impregnating a lithium aluminium silicate support having an HPA wash-coat in a solution of (NH 3 ) 4 Pt ⁇ Cl 2 .
- the impregnated support was dried at 120°C, and calcined at 450°C .
- the catalyst was then calcined in air at 1200°C for 6 hours.
- the catalyst was analysed and found to have 0.86 wt % Pt.
- a catalyst comprising Pt and Sn was prepared by impregnating a lithium aluminium silicate support having an HPA wash-coat in a solution of 1) (NH 3 )4Pt ⁇ Cl 2 , and 2) SnCl 2 /HCl.
- the impregnated support was dried, calcined and reduced as described in connection with Example 1 above.
- the catalyst was analysed and found to have 0.48 wt % Pt, and 2.80 wt % Sn.
- Example 2 The catalysts of Example 1, Comparative Example A and Comparative Example
- the catalyst was prepared by sequential impregnation of 30ppi ceramic foam blocks (lithium aluminium silicate with alumina washcoat) with aqueous tetrammineplatinum(II) chloride and germanium tetrachloride in ethanol. Between impregnations the blocks were dried in air at 120-140°C for ca. 30 minutes then calcined in air at 450°C for 30 minutes, cooled to room temperature and the impregnation procedure was repeated. Once all the impregnation solution had been absorbed onto the foam the blocks were calcined in air at 600°C for 6 hours. Several of the calcined blocks were given a further air calcination at 1200°C for 6
- the catalyst comprised 1.0 wt % Pt and 4.0 wt % Ge.
- Example 3 The catalyst of Example 3 was tested as a catalyst for the oxidative dehydrogenation of ethane using the apparatus of Figure 1.
- the reactor employed was formed of quartz.
- the performance of this catalyst was compared to that of Comparative Example A.
- the dehydrogenation conditions employed are summarised in Table 3 below.
- Table 4 shows the ethane conversion and selectivities achieved.
- the catalyst was prepared by sequential impregnation of 30ppi ceramic foam block (99.5%o alumina with alumina washcoat) with aqueous tetrammineplatinum(II) chloride and aqueous gallium nitrate.
- the foam block employed was 28mm diameter and 30mm in depth. Between impregnations, the block was dried in air at 120-140°C for ca. 30 minutes, calcined in air at 450°C for 30 minutes, and then cooled to room temperature. Once all the impregnation solution had been absorbed onto the foam block, the block was calcined in air at 600°C for 6 hours.
- the Pt and Ga solutions were prepared with sufficient salt to achieve final Pt/Ga loadings of 0.28 wt%> platinum and 0.75 wt% gallium.
- the atomic platinum:gallium ratio was 1 :7.5.
- Example 5 The catalysts of Example 5, and Comparative Example A were tested as catalysts for the oxidative dehydrogenation of ethane. Each catalyst was mounted in the apparatus of Figure 1, and an oxidative dehydrogenation reaction was carried out under the conditions summarised in Table 5 below.
- the catalyst was prepared by sequential impregnation of 30ppi ceramic foam blocks
- foam block used was 28mm in diameter and 30mm in depth Between impregnations, the block was dried in air at 120-140°C for ca 30 minutes, calcined in air at 450°C for 30 minutes, and then cooled to room temperature
- Example 7 a Pt/In catalyst was prepared in the manner of Example 7 above, except that the catalyst was calcined in air at 1200°C for 6 hours, rather than at 600°C
- Example 7 The catalysts of Example 7, 8 and Comparative Example A were tested as catalysts for the oxidative dehydrogenation of ethane Each catalyst was mounted in the apparatus of Figure 1, and an oxidative dehydrogenation reaction was carried out under the conditions summarised in Table 7 below
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
Abstract
Description
Claims
Priority Applications (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2001549318A JP2003519105A (en) | 1999-12-23 | 2000-12-14 | Olefin production method |
AU21965/01A AU777050B2 (en) | 1999-12-23 | 2000-12-14 | Process for the production of olefins |
AT00985554T ATE297367T1 (en) | 1999-12-23 | 2000-12-14 | METHOD FOR PRODUCING OLEFINS |
DE60020733T DE60020733T2 (en) | 1999-12-23 | 2000-12-14 | PROCESS FOR THE PRODUCTION OF OLEFINES |
CA002395376A CA2395376A1 (en) | 1999-12-23 | 2000-12-14 | Process for the production of olefins |
BR0016603-0A BR0016603A (en) | 1999-12-23 | 2000-12-14 | Process for olefin production |
EP00985554A EP1240120B8 (en) | 1999-12-23 | 2000-12-14 | Process for the production of olefins |
NO20023045A NO20023045L (en) | 1999-12-23 | 2002-06-21 | Process for producing olefins |
AU2004242502A AU2004242502A1 (en) | 1999-12-23 | 2004-12-30 | Process for the production of olefins |
US11/253,817 US20060069297A1 (en) | 1999-12-23 | 2005-10-20 | Process for the production of olefins |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GBGB9930598.9A GB9930598D0 (en) | 1999-12-23 | 1999-12-23 | Process for production of olefins |
GB9930598.9 | 1999-12-23 | ||
GB0006386A GB0006386D0 (en) | 2000-03-16 | 2000-03-16 | Process for production of olefins |
GB0006386.7 | 2000-03-16 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US11/253,817 Continuation US20060069297A1 (en) | 1999-12-23 | 2005-10-20 | Process for the production of olefins |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2001047842A1 true WO2001047842A1 (en) | 2001-07-05 |
Family
ID=26243887
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB2000/004794 WO2001047842A1 (en) | 1999-12-23 | 2000-12-14 | Process for the production of olefins |
Country Status (13)
Country | Link |
---|---|
US (2) | US20030055306A1 (en) |
EP (2) | EP1240120B8 (en) |
JP (1) | JP2003519105A (en) |
CN (1) | CN1250491C (en) |
AT (1) | ATE297367T1 (en) |
AU (2) | AU777050B2 (en) |
BR (1) | BR0016603A (en) |
CA (1) | CA2395376A1 (en) |
DE (1) | DE60020733T2 (en) |
GC (1) | GC0000162A (en) |
MY (1) | MY127818A (en) |
NO (1) | NO20023045L (en) |
WO (1) | WO2001047842A1 (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7067455B2 (en) | 2003-11-21 | 2006-06-27 | Conocophillips Company | Copper modified catalysts for oxidative dehydrogenation |
WO2006077368A1 (en) * | 2005-01-21 | 2006-07-27 | Ineos Europe Limited | Process for the production of olefins by autothermal cracking |
US7807860B2 (en) | 2003-02-18 | 2010-10-05 | Ineos Europe Limited | Autothermal cracking process and reactor |
US9782754B2 (en) | 2012-07-26 | 2017-10-10 | Saudi Basic Industries Corporation | Alkane dehydrogenation catalyst and process for its preparation |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100404129C (en) * | 2005-10-25 | 2008-07-23 | 中国石油天然气股份有限公司 | Catalyst for removing hydrocarbon impurities in carbon dioxide, preparation method and application |
EP1820569A1 (en) * | 2006-01-20 | 2007-08-22 | Ineos Europe Limited | Process for contacting a hydrocarbon and an oxygen-containing gas with a catalyst bed |
US9963407B2 (en) | 2013-06-18 | 2018-05-08 | Uop Llc | Fluidized catalyst circulation reactor for paraffin oxydative dehydrogenation |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3437703A (en) * | 1966-05-05 | 1969-04-08 | Foster Grant Co Inc | Catalytic dehydrogenation process and compositions |
US4788371A (en) * | 1987-12-30 | 1988-11-29 | Uop Inc. | Catalytic oxidative steam dehydrogenation process |
WO1994004632A1 (en) * | 1992-08-20 | 1994-03-03 | Bp Chemicals Limited | Process for the production of mono-olefins |
WO2000014037A1 (en) * | 1998-09-03 | 2000-03-16 | The Dow Chemical Company | On-line synthesis and regeneration of a catalyst used in autothermal oxidation |
Family Cites Families (8)
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US3123574A (en) * | 1964-03-03 | Hydrogenation of cottonseed and soybean oils foe shortening stock | ||
US3670044A (en) * | 1969-07-18 | 1972-06-13 | Phillips Petroleum Co | Catalytic dehydrogenation process |
US3856880A (en) * | 1970-03-02 | 1974-12-24 | Petro Tex Chem Corp | Oxidative dehydrogenation catalyzed with promoted zinc ferrite |
BE789153A (en) * | 1971-09-23 | 1973-03-22 | Aquitaine Petrole | IMPROVEMENT IN THE MANUFACTURE OF STYRENE |
US4435607A (en) * | 1981-04-28 | 1984-03-06 | Uop Inc. | Dehydrogenation of dehydrogenatable hydrocarbons |
CA1211131A (en) * | 1981-04-28 | 1986-09-09 | Tamotsu Imai | Dehydrogenation of dehydrogenatable hydrocarbons |
DE3210708A1 (en) * | 1982-03-24 | 1983-10-06 | Basf Ag | CATALYST AND ITS USE FOR PRODUCING METHYL METHACRYLATE |
JPH05194281A (en) * | 1992-01-23 | 1993-08-03 | Nippon Oil Co Ltd | Method for dehydrating hydrocarbons |
-
2000
- 2000-12-14 JP JP2001549318A patent/JP2003519105A/en not_active Withdrawn
- 2000-12-14 CA CA002395376A patent/CA2395376A1/en not_active Abandoned
- 2000-12-14 DE DE60020733T patent/DE60020733T2/en not_active Expired - Fee Related
- 2000-12-14 US US10/168,482 patent/US20030055306A1/en not_active Abandoned
- 2000-12-14 CN CNB008190844A patent/CN1250491C/en not_active Expired - Fee Related
- 2000-12-14 BR BR0016603-0A patent/BR0016603A/en not_active IP Right Cessation
- 2000-12-14 WO PCT/GB2000/004794 patent/WO2001047842A1/en active IP Right Grant
- 2000-12-14 EP EP00985554A patent/EP1240120B8/en not_active Expired - Lifetime
- 2000-12-14 AT AT00985554T patent/ATE297367T1/en not_active IP Right Cessation
- 2000-12-14 EP EP05076241A patent/EP1616847A1/en not_active Withdrawn
- 2000-12-14 AU AU21965/01A patent/AU777050B2/en not_active Ceased
- 2000-12-21 MY MYPI20006074A patent/MY127818A/en unknown
-
2001
- 2001-01-06 GC GCP20011119 patent/GC0000162A/en active
-
2002
- 2002-06-21 NO NO20023045A patent/NO20023045L/en not_active Application Discontinuation
-
2004
- 2004-12-30 AU AU2004242502A patent/AU2004242502A1/en not_active Abandoned
-
2005
- 2005-10-20 US US11/253,817 patent/US20060069297A1/en not_active Abandoned
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3437703A (en) * | 1966-05-05 | 1969-04-08 | Foster Grant Co Inc | Catalytic dehydrogenation process and compositions |
US4788371A (en) * | 1987-12-30 | 1988-11-29 | Uop Inc. | Catalytic oxidative steam dehydrogenation process |
WO1994004632A1 (en) * | 1992-08-20 | 1994-03-03 | Bp Chemicals Limited | Process for the production of mono-olefins |
WO2000014037A1 (en) * | 1998-09-03 | 2000-03-16 | The Dow Chemical Company | On-line synthesis and regeneration of a catalyst used in autothermal oxidation |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7807860B2 (en) | 2003-02-18 | 2010-10-05 | Ineos Europe Limited | Autothermal cracking process and reactor |
US7067455B2 (en) | 2003-11-21 | 2006-06-27 | Conocophillips Company | Copper modified catalysts for oxidative dehydrogenation |
WO2006077368A1 (en) * | 2005-01-21 | 2006-07-27 | Ineos Europe Limited | Process for the production of olefins by autothermal cracking |
US9782754B2 (en) | 2012-07-26 | 2017-10-10 | Saudi Basic Industries Corporation | Alkane dehydrogenation catalyst and process for its preparation |
Also Published As
Publication number | Publication date |
---|---|
GC0000162A (en) | 2005-06-29 |
CA2395376A1 (en) | 2001-07-05 |
NO20023045L (en) | 2002-08-16 |
JP2003519105A (en) | 2003-06-17 |
US20030055306A1 (en) | 2003-03-20 |
ATE297367T1 (en) | 2005-06-15 |
DE60020733D1 (en) | 2005-07-14 |
EP1240120B8 (en) | 2005-08-10 |
EP1616847A1 (en) | 2006-01-18 |
US20060069297A1 (en) | 2006-03-30 |
EP1240120A1 (en) | 2002-09-18 |
AU2004242502A1 (en) | 2005-01-27 |
CN1434790A (en) | 2003-08-06 |
CN1250491C (en) | 2006-04-12 |
AU777050B2 (en) | 2004-09-30 |
EP1240120B1 (en) | 2005-06-08 |
AU2196501A (en) | 2001-07-09 |
BR0016603A (en) | 2003-06-10 |
NO20023045D0 (en) | 2002-06-21 |
MY127818A (en) | 2006-12-29 |
DE60020733T2 (en) | 2006-05-18 |
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