WO2017001445A1 - Catalyseur de conversion d'hydrocarbure pour produire un produit d'hydrocarbure moins saturé - Google Patents

Catalyseur de conversion d'hydrocarbure pour produire un produit d'hydrocarbure moins saturé Download PDF

Info

Publication number
WO2017001445A1
WO2017001445A1 PCT/EP2016/065084 EP2016065084W WO2017001445A1 WO 2017001445 A1 WO2017001445 A1 WO 2017001445A1 EP 2016065084 W EP2016065084 W EP 2016065084W WO 2017001445 A1 WO2017001445 A1 WO 2017001445A1
Authority
WO
WIPO (PCT)
Prior art keywords
mass fraction
catalyst
range
hydrocarbon
mixtures
Prior art date
Application number
PCT/EP2016/065084
Other languages
English (en)
Inventor
Kongkiat Suriye
Amnart Jantharasuk
Wuttithep Jareewatchara
Original Assignee
SMH Co., Ltd.
Scholz, Volker
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by SMH Co., Ltd., Scholz, Volker filed Critical SMH Co., Ltd.
Publication of WO2017001445A1 publication Critical patent/WO2017001445A1/fr

Links

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
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • 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
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/652—Chromium, molybdenum or tungsten
    • B01J23/6527—Tungsten
    • 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
    • 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
    • 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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • 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
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/656—Manganese, technetium or rhenium
    • B01J23/6562—Manganese
    • 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
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8993—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with chromium, molybdenum or tungsten
    • 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
    • B01J23/90—Regeneration or reactivation
    • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
    • 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
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/12—Treating with free oxygen-containing gas
    • 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
    • C07C2523/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of rare earths
    • 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
    • C07C2523/14—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of germanium, tin or lead
    • 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
    • C07C2523/30—Tungsten
    • 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
    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/42—Platinum
    • 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
    • C07C2523/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tatalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/652—Chromium, molybdenum or tungsten
    • 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
    • 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

Definitions

  • the present invention relates to a catalyst for hydrocarbon conversion. More specifically, the present invention is directed to a catalyst for converting a hydrocarbon feed to a less saturated hydrocarbon product.
  • Olefins especially light olefins including ethylene and propylene, are valuable hydrocarbon products. They are useful for preparing a wide variety of end products, including ethylene oxide, propylene oxide, ethylbenzene, acetone, phenol, polyethylene, polypropylene, other polymers, and other petrochemical products. Even though their prices have been fluctuated over time, their demands in the industry have still been continuously growing.
  • US 8,198,498 B2 disclosed a carbon nanotube catalyst coated with metal oxides for using in hydrocarbon cracking process.
  • the process is still highly energy intensive because it has to be carried out at quite high temperatures, and preferably with addition of steam to the feed stream, in order to achieve improved yield of the desirable olefins product.
  • it is the object to provide a catalyst for converting a hydrocarbon feed to a less saturated hydrocarbon product which may be operated under mild conditions, in particular at comparably low temperatures, but which allows to produce the less saturated hydrocarbon product with high selectivity to achieve the desired product.
  • the present invention provides a catalyst in oxidic form comprising metals Ml, M2, M3 and M4, wherein:
  • Ml is selected from Si, Al, Zr, and mixtures thereof;
  • M2 is selected from Pt, Cr, and mixtures thereof;
  • M3 is selected from W, Mo, Re, and mixtures thereof;
  • M4 is selected from Sn, K, Y, Yb and mixtures thereof; wherein mass fraction of Ml is in the range of 0.1 to 0.8; mass fraction of M2 is in the range of 0.001 to 0.2; mass fraction of M3 is in the range of 0.001 to 0.2; mass fraction of M4 is in the range of 0.0001 to 0.2; and mass fraction of oxygen is in the range of 0.1 to 0.8.
  • the inventive catalyst allows converting a hydrocarbon feed to olefins products with high selectivity and at relatively mild conditions.
  • the inventive catalyst is a hydrocarbon conversion catalyst, i.e. a catalyst for use in a hydrocarbon conversion process, being a multi-metal composition comprising:
  • Ml is selected from Si, Al, Zr, and mixtures thereof; M2 is selected from Pt, Cr, and mixtures thereof, preferably Pt; M3 is selected from W, Mo, Re, and mixtures thereof, preferably W; M4 is selected from Sn, K, Y, Yb and mixtures thereof; and oxygen; wherein mass fraction of Ml is in the range of 0.1 to 0.8, preferably 0.2 to 0.6; mass fraction of M2 is in the range of 0.001 to 0.2, preferably 0.0015 to 0.15, more preferably 0.005 to 0.1; mass fraction of M3 is in the range of 0.001 to 0.2, preferably 0.005 to 0.15, more preferably 0.01 to 0.1; mass fraction of M4 is in the range ofO.0001 to 0.2, preferably 0.00015 to 0.03, more preferably 0.005 to 0.02; and mass fraction of oxygen is in the range of 0.1 to 0.8, preferably 0.2 to 0.5.
  • mass fraction is related to the total mass (weight) of the inventive catalyst.
  • the catalyst has preferably the formula M1M2M3M40.
  • the inventive catalyst further comprises M5 (i.e. is a catalyst having the formula M1M2M3M4M50), wherein M5 is selected from Mg, Ca, Mn, Fe, Co, Ni, Cu, , and mixtures thereof, preferably Mg, Ca, and mixture thereof; and mass fraction of M5 is in the range of 0.005 to 0.1 , preferably 0.01 to 0.09.
  • M5 i.e. is a catalyst having the formula M1M2M3M4M50
  • M5 is selected from Mg, Ca, Mn, Fe, Co, Ni, Cu, , and mixtures thereof, preferably Mg, Ca, and mixture thereof
  • mass fraction of M5 is in the range of 0.005 to 0.1 , preferably 0.01 to 0.09.
  • the inventive catalyst can be prepared by mixing all precursors of the element Ml to M5 together followed by a suitable heat treatment in order to obtain the desired multi-metal composition.
  • Element precursors are starting compounds containing the desired elements which can be converted to the desired form of elements, preferably oxides, in the final catalyst by a suitable heat treatment.
  • precursor to Ml to M5 may include oxides, halides, alkoxide, nitrates, carbonates, formate, oxalates, amine, or hydroxides of the elements.
  • element precursors can occur in dry form or wet form.
  • the element precursors may conveniently be provided in powder form. Powder of the element precursors can be easily mixed by physical mixing in a blender.
  • the element precursors' mixture is then subjected to a suitable heat treatment, preferably calcination, to obtain the final hydrocarbon conversion catalyst.
  • the element precursors may be provided in solution and/or suspension form.
  • a mixture of the element precursors' solutions and/or suspensions is then dried to remove the solvents. Subsequently, the dried mixture is subjected to a suitable heat treatment, preferably calcination, to obtain the final catalyst.
  • some of the element precursors are provided in dry form and some of the element precursors are provided in wet form.
  • the dry and wet element precursors can be combined by conventional methods including
  • the obtained mixture is then subjected to a suitable heat treatment, preferably calcination, to obtain the final catalyst.
  • a suitable heat treatment involves a selected atmosphere and a selected temperature capable of removing and/or converting at least a part of the element precursors to the desired form of the corresponding elements in the final catalyst. Particularly preferred is the elements are in oxides form in the final catalyst.
  • the selected atmosphere may include oxidizing atmosphere, reducing atmosphere, and inert atmosphere.
  • the prepared catalyst powder is subjected to calcination in air at a temperature in the range of 300°C to 800°C for 1 to 24 hours, even more preferably 400°C to 600°C for 2 to 10 hours
  • preparation of the catalyst according to the present invention may further involve forming the catalyst powder into a shape suitable for a commercial reactor.
  • Shapes suitable for a commercial reactor may include pellets, extrudates, spheres, and the like.
  • Sufficient binder materials may be further added to the catalyst composition to facilitate forming of the catalyst. Providing the catalyst in a specific shape allows more easy use thereof.
  • the inventive catalyst can be used in a hydrocarbon conversion process wherein a hydrocarbon feed stream is contacted with the inventive catalyst.
  • the hydrocarbon feed stream comprises a paraffmic hydrocarbon.
  • the hydrocarbon feed stream comprises a paraffin having 2 to 5 carbon atoms.
  • the hydrocarbon feed stream comprises a paraffin selected from ethane, propane, butane, pentane and mixtures thereof, preferably propane, butane, and a mixture thereof.
  • the hydrocarbon conversion process is carried out at a temperature in the range of 200°C to 700°C, preferably 300°C to 600°C, even more preferably 350°C to 550°C.
  • the inventive catalyst allows to drive the hydrocarbon conversion process at the before mentioned preferred temperatures which are comparably low with respect to the processes know in the art.
  • the process is carried out at a pressure in the range of 0.01 to 10 bar gauge, preferably 0.05 to 5 bar gauge.
  • the contact time needed to obtain a desirable yield of olefins product depends upon several factors such operating temperature, operating pressure, and catalyst activity. In an
  • the process is carried out at a weight hourly space velocity (WHS V) in the range of 0.01 to 20 hr "1 , preferably 0.05 to 5 hr 1 .
  • WHS V weight hourly space velocity
  • the process can be conducted in a batch manner or a continuous manner. For commercial scale, it is favorable that the process is continuously operated. Continuous operation can be performed with fixed bed, fluidized bed, or other techniques known in the art with fixed bed being typically preferred.
  • the catalyst Prior to contacting with the hydrocarbon feed stream, the catalyst may optionally be pretreated.
  • the pretreatment condition may include contacting the catalyst with an inert gas, an oxidizing gas, a reducing gas, a hydrocarbon, preferably a C2-C6 aliphatic hydrocarbon, and any mixture thereof .
  • the pretreatment may be divided into several steps wherein each step may employ different conditions and atmospheres. It is generally preferred that the pretreatment is performed at a heated temperature, preferably 200°C to 700°C, more preferably 300°C to 600°C, even more preferably 350°C to 550°C.
  • the hydrocarbon conversion process comprises a regeneration step wherein the regeneration step includes contacting the hydrocarbo conversion catalyst with an oxidizing agent at a high temperature. The regeneration step should be carefully controlled to avoid overheating and destroying structure of the catalyst.
  • the regeneration step includes contacting the hydrocarbo conversion catalyst with an oxidizing agent at a high temperature. The regeneration step should be carefully controlled to avoid overheating and destroying structure of the catalyst.
  • regeneration step is carried out at a temperature in the range of 200°C to 700° C, preferably 300°C to 600°C.
  • Other known regeneration techniques can be employed without limitation.
  • the inventive catalyst according to the present invention is capable of converting light paraffin feed with high selectivity to light olefins, including ethylene, propylene, and butenes. Significantly low amount of less valued by-products such as methane and heavier
  • hydrocarbons are produced.
  • a zeolite catalyst containing 0.95 mass fraction of Si and 0.05 mass fraction of Al was contacted with propane at 475°C, 1 bar gauge, and WHSV of 0.12 h "1 . Results of this reaction at time on stream 3 hours and 8 hours are displayed in Table 1.
  • Example 2 (comparative) A catalyst containing 0.5 mass fraction of Al, 0.45 mass fraction of O, and 0.05 mass fraction of Pt was contacted with propane at 475°C, 1 bar gauge, and WHSV of 0.12 h "1 Results of this reaction at time on stream 3 hours and 8 hours are displayed in Table 1.
  • a catalyst containing 0.306 mass fraction of Si, 0.012 mass fraction of Al, 0.031 mass fraction of Mg, 0.044 mass fraction of W, 0.387 mass fraction of O, 0.189 mass fraction of Zr, 0.02 mass fraction of Pt, and 0.011 mass fraction of Y was contacted with propane at 475°C, 1 bar gauge, and WHSV of 0.12 h "1 . Results of this reaction at time on stream 3 hours and 8 hours are displayed in Table 1.
  • a catalyst containing 0.248 mass fractio of Si, 0.213 mass fraction of Al, 0.031 mass fraction of Mg, 0.044 mass fraction of W, 0.433 mass fraction of 0, 0.02 mass fraction of Pt, and 0.01 1 mass fraction of K was contacted with propane at 475°C, 1 bar gauge, and WHSV of 0.12 fa "1 . Results of this reaction at time on stream 3 hours and 8 hours are displayed in Table 1.
  • the selectivity of total olefins was calculated from selectivity of olefin products including ethylene, propylene, and butenes.

Landscapes

  • 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)
  • Catalysts (AREA)

Abstract

La présente invention concerne un catalyseur sous forme d'oxyde comprenant des métaux M1, M2, M3 et M4, M1 étant choisi parmi Si, Al, Zr et des mélanges de ceux-ci ; M2 étant choisi parmi Pt, Cr et des mélanges de ceux-ci ; M3 étant choisi parmi W, Mo, Re et des mélanges de ceux-ci ; et M4 étant choisi parmi Sn, K, Y, Yb et des mélanges de ceux-ci ; la fraction massique de M1 étant dans la plage de 0,1 à 0,8 ; la fraction massique de M2 étant dans la plage de 0,001 à 0,2 ; la fraction massique de M3 étant dans la plage de 0,001 à 0,2 ; la fraction massique de M4 étant dans la plage de 0,0001 à 0,2. Le catalyseur est utile pour convertir une charge d'hydrocarbure en un produit d'hydrocarbure moins saturé.
PCT/EP2016/065084 2015-06-29 2016-06-29 Catalyseur de conversion d'hydrocarbure pour produire un produit d'hydrocarbure moins saturé WO2017001445A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP15174320 2015-06-29
EP15174320.0 2015-06-29

Publications (1)

Publication Number Publication Date
WO2017001445A1 true WO2017001445A1 (fr) 2017-01-05

Family

ID=53524595

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2016/065084 WO2017001445A1 (fr) 2015-06-29 2016-06-29 Catalyseur de conversion d'hydrocarbure pour produire un produit d'hydrocarbure moins saturé

Country Status (2)

Country Link
TW (1) TW201707788A (fr)
WO (1) WO2017001445A1 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3649566A (en) * 1970-01-12 1972-03-14 Universal Oil Prod Co Dehydrogenation catalysts containing platinum rhenium a group vi transition metal and an alkali or alkaline earth metal
US3980721A (en) * 1971-11-19 1976-09-14 Institut Francaise Du Petrole, Des Carburants Et Lubrifiants Et Entreprise De Recherches Et D'activites Petrolieres Elf Catalyst particularly useful for dehydrogenating saturated hydrocarbons
US20110257443A1 (en) * 2010-02-02 2011-10-20 Celanese International Corporation Catalyst Supports Having Crystalline Support Modifiers
US8198498B2 (en) 2010-08-19 2012-06-12 Kamyar Keyvanloo Carbon nanotube catalyst for olefin production
US20130178661A1 (en) * 2012-01-06 2013-07-11 Celanese International Corporation Hydrogenation Catalysts with Cobalt-Modified Supports
CN104107712A (zh) * 2013-04-16 2014-10-22 中国石油化工股份有限公司 混合c3/c4烷烃脱氢催化剂及其制备方法
US8933286B2 (en) 2008-11-25 2015-01-13 Petroleo Brasileiro S.A.—Petrobras Catalytic cracking process of a stream of hydrocarbons for maximization of light olefins

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3649566A (en) * 1970-01-12 1972-03-14 Universal Oil Prod Co Dehydrogenation catalysts containing platinum rhenium a group vi transition metal and an alkali or alkaline earth metal
US3980721A (en) * 1971-11-19 1976-09-14 Institut Francaise Du Petrole, Des Carburants Et Lubrifiants Et Entreprise De Recherches Et D'activites Petrolieres Elf Catalyst particularly useful for dehydrogenating saturated hydrocarbons
US8933286B2 (en) 2008-11-25 2015-01-13 Petroleo Brasileiro S.A.—Petrobras Catalytic cracking process of a stream of hydrocarbons for maximization of light olefins
US20110257443A1 (en) * 2010-02-02 2011-10-20 Celanese International Corporation Catalyst Supports Having Crystalline Support Modifiers
US8198498B2 (en) 2010-08-19 2012-06-12 Kamyar Keyvanloo Carbon nanotube catalyst for olefin production
US20130178661A1 (en) * 2012-01-06 2013-07-11 Celanese International Corporation Hydrogenation Catalysts with Cobalt-Modified Supports
CN104107712A (zh) * 2013-04-16 2014-10-22 中国石油化工股份有限公司 混合c3/c4烷烃脱氢催化剂及其制备方法

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
JESPER J. H. B. SATTLER ET AL: "Catalytic Dehydrogenation of Light Alkanes on Metals and Metal Oxides", CHEMICAL REVIEWS, vol. 114, no. 20, 22 October 2014 (2014-10-22), US, pages 10613 - 10653, XP055237672, ISSN: 0009-2665, DOI: 10.1021/cr5002436 *
LIHUI WAN ET AL: "Influence of Lanthanum Addition on Catalytic Properties of PtSnK/Al 2 O 3 Catalyst for Isobutane Dehydrogenation", INDUSTRIAL & ENGINEERING CHEMISTRY RESEARCH., vol. 50, no. 8, 20 April 2011 (2011-04-20), US, pages 4280 - 4285, XP055237670, ISSN: 0888-5885, DOI: 10.1021/ie1023518 *

Also Published As

Publication number Publication date
TW201707788A (zh) 2017-03-01

Similar Documents

Publication Publication Date Title
JP6289607B2 (ja) パラフィンをオレフィンに転化するためのプロセス及びそこで使用するための触媒
US11286218B2 (en) Hydrocarbon conversion process
US10472304B2 (en) Catalyst and hydrocarbon conversion process utilizing the catalyst
JP6446033B2 (ja) 不飽和炭化水素の製造方法
US11285461B2 (en) Catalyst system and process utilizing the catalyst system
US11383225B2 (en) Hydrocarbon conversion catalyst system
EP3335792B1 (fr) Système catalyseur et procédé de conversion d'une charge d'hydrocarbure utilisant le système catalyseur
US10336947B2 (en) Process for conversion of a hydrocarbon feed
WO2017001445A1 (fr) Catalyseur de conversion d'hydrocarbure pour produire un produit d'hydrocarbure moins saturé
JP6527364B2 (ja) ブタジエンを含む生成物の製造方法
JP7018174B2 (ja) 芳香族炭化水素の製造方法
US11318445B2 (en) Hydrocarbon conversion catalyst
JP2019059704A (ja) 芳香族化合物の製造方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16733501

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 16733501

Country of ref document: EP

Kind code of ref document: A1