US20100298129A1 - selective nickel based hydrogenation catalyst and the preparation thereof - Google Patents

selective nickel based hydrogenation catalyst and the preparation thereof Download PDF

Info

Publication number
US20100298129A1
US20100298129A1 US12/741,017 US74101708A US2010298129A1 US 20100298129 A1 US20100298129 A1 US 20100298129A1 US 74101708 A US74101708 A US 74101708A US 2010298129 A1 US2010298129 A1 US 2010298129A1
Authority
US
United States
Prior art keywords
catalyst
carrier
oxide
nickel
hours
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US12/741,017
Other languages
English (en)
Inventor
Shunqin Liang
Ying Qian
Longgang Lv
Limin Sun
Yundi Zheng
Tinghai Wang
Jie Wu
Fengxia Cao
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Petrochina Co Ltd
Original Assignee
Petrochina Co Ltd
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 Petrochina Co Ltd filed Critical Petrochina Co Ltd
Assigned to PETROCHINA COMPANY LIMITED reassignment PETROCHINA COMPANY LIMITED ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WANG, TINGHAI, CAO, FENGXIA, LIANG, SHUNQIN, LV, LONGGANG, QIAN, YING, SUN, LIMIN, WU, JIE, ZHENG, YUNDI
Publication of US20100298129A1 publication Critical patent/US20100298129A1/en
Abandoned legal-status Critical Current

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
    • B01J23/70—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
    • B01J23/83—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 with rare earths or actinides
    • 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
    • B01J23/84—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 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/888—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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/12—Silica and alumina
    • 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
    • B01J23/84—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 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—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
    • B01J23/70—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
    • B01J23/84—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 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/86—Chromium
    • B01J23/866—Nickel and chromium
    • 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
    • B01J23/84—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 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8871—Rare earth metals or actinides
    • 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
    • B01J23/84—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 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8872—Alkali or alkaline earth 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/633—Pore volume less than 0.5 ml/g
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/635—0.5-1.0 ml/g
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B01J37/0207—Pretreatment of the support
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/024—Multiple impregnation or coating
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • 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
    • B01J23/78—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 with alkali- or alkaline earth 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Definitions

  • the present invention relates to a selective nickel-based hydrogenation catalyst and the preparation thereof.
  • the catalyst is useful in selective hydrogenation of medium or low distillate oil, in particular, in the first-stage selective hydrogenation process of pyrolysis gasoline distillate.
  • Pyrolysis gasoline is the by-product of steam cracking to make ethylene, which approximately comprises more than 50% of the production capacity of ethylene.
  • Pyrolysis gasoline contains highly unsaturated hydrocarbons, such as diolefin, styrene and the like, which can be converted into corresponding monoolefin by selective hydrogenation.
  • the hydrogenation of pyrolysis gasoline has developed toward the hydrogenation of full distillate using nickel-based catalyst.
  • the pyrolysis gasoline raw materials Due to the variability of the pyrolysis gasoline raw materials and the differences in pyrolysis apparatus and pyrolysis modes, the pyrolysis gasoline raw materials are deteriorated, and the hydrogenation load and the content of impurity such as arsenic are increased, thereby causing the inferior performance of palladium-based catalyst for first-stage hydrogenation.
  • the pyrolysis gasoline raw materials are deteriorated, and the hydrogenation load and the content of impurity such as arsenic are increased, thereby causing the inferior performance of palladium-based catalyst for first-stage hydrogenation.
  • For noble metal catalyst its arsenic and colloid resistance as well as water resistance is low, since the impurity arsenic tends to occupy the empty orbital of Pd, and Pd is located on the surface layer of the catalyst with a content of only parts per thousand.
  • non-noble metal catalyst For non-noble metal catalyst, it has certain arsenic tolerance and colloid and water resistance due to the structural difference and high metal content; moreover, it has relatively remarkable price advantage. Thus, there is need of the market and technical competition to develop a new nickel-based catalyst for first-stage hydrogenation of full distillate pyrolysis gasoline.
  • U.S. Pat. No. 3,472,763 reports a Ni/Al 2 O 3 catalyst for the selective hydrogenation of diolefin, comprising 1-20% nickel as active component, 1-5% MoO 3 as aids, 1-5% alkali metal and alkaline earth metal as aids, and having a pore volume of more than 0.4 ml/g and a specific surface area of more than 30 m 2 /g.
  • This catalyst is prepared by impregnating the Al 2 O 3 carrier with the aqueous solution of above-mentioned active component and aids.
  • CN1218822A reports a Ni/Al 2 O 3 catalyst suitable for the selective hydrogenation of pyrolysis gasoline distillates. This catalyst is prepared by loading nickel on alumina carrier comprising lithium or alkaline earth metal. However, this catalyst is not good at withstanding the hydrogenation load and its hydrogenation stability is to be improved.
  • An excellent selective hydrogenation catalyst should have higher hydrogenation activity and better selectivity. More importantly, it should have good stability. That is to say, it is necessary for such catalyst to have capability to resist impurity and colloid, thereby prolonging its lifetime.
  • the aim of the present invention is to develop a nickel-based Al 2 O 3 supported catalyst for selective hydrogenation of diolefin.
  • the catalyst has good hydrogenation performance, especially has good hydrogenation stability, and can be applied to the selective hydrogenation of full distillate pyrolysis gasoline.
  • the selective nickel-based hydrogenation catalyst of the present invention is characterized in that based on the total weight of the catalyst, it comprises:
  • said catalyst has a specific surface area of 60-150 m 2 /g and a pore volume of 0.4-0.6 ml/g.
  • This catalyst is especially useful in the diolefin selective hydrogenation of medium or low distillate oil, in particular, in the diolefin selective hydrogenation of full distillate pyrolysis gasoline.
  • the present invention also provides a method for preparing such catalyst, comprising:
  • the present invention preferably recommends that the modified alumina carrier is prepared by:
  • the catalyst according to the present invention comprises 2-8% silica, which may increase the stability of the catalyst, especially the carrier during calcination.
  • the content of silica is 3-4%.
  • the content of nickel oxide is 15-19%.
  • the catalyst according to the present invention comprises alkaline earth metal, which may adjust the acidity of the catalyst after calcination and improve the colloid resistance during hydrogenation reaction.
  • the alkaline earth metal is magnesium and/or strontium.
  • the content of alkaline earth metal oxide is preferably 2-5%.
  • the lanthanum and/or cerium are added in the form of nitrate dissolved in the impregnating solution so as to improve the hydrogenation activity and stability of the catalyst.
  • the content of lanthanum oxide and/or cerium oxide is 3-5%.
  • the VIB group element is added to improve the hydrogenation activity and impurity (for example, sulfur) resistance of the catalyst.
  • the VIB group element is one or more of Cr, Mo and W.
  • the content of VIB group element oxide is preferably 3-6%.
  • the solution of the active component and aids are impregnated onto the resultant catalyst carrier in twice to increase the dispersity of the active component of the catalyst and improve the activity and stability of catalyst.
  • the compounds of nickel (as active component), magnesium, strontium lanthanum and cerium (as aids) in above-mentioned preparation process may be in the form of sulfate, nitrate and halide and so on. Preferably, they are in the form of nitrate, since nitrate is easily soluble in water to be fully dissolved and form stable solution.
  • the alumina hydrate as the starting material for preparing the catalyst according to the present invention, may be alumina hydrates prepared by carbon dioxide method, ammonia method, and nitric acid method and so on.
  • the alumina hydrate prepared by nitric acid method is preferable due to its better hydrogenation performance.
  • the catalyst according to the present invention should be reduced under hydrogen at the temperature of 350-400° C. for 5-6 hours prior to use. During the reduction, the volume ratio of hydrogen to catalyst is 150:1 to 500:1.
  • Nickel nitrate available from Xi′ an Chemical Reagent Factory
  • Magnesium nitrate and strontium nitrate available from Shanghai Colloid Chemical Plant;
  • Cerium nitrate and lanthanum nitrate available from Shensheng Reagent Factory, Fufeng, Yixing, Jiangsu;
  • Alumina powder available from Lanhua Xiangxin Additives Factory.
  • alumina carrier 140 ml water, 5 ml nitric acid (the content of which is 60%) and 16 ml silica sol (comprising 40% silica) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and then calcinated at 560° C. for 4 hours. 100 g calcinated carrier is impregnated with a solution form by dissolving 26 g magnesium nitrate into water, dried in air at 120° C., and calcinated at 1050° C. for 4 hours, thereby obtaining the modified Al 2 O 3 carrier.
  • 10 g nickel nitrate is added to 20 ml water with stirring. While stirring, 2.1 g cerium nitrate and 0.3 g ammonium molybdate are added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 400° C. for 4 hours, thereby obtaining the catalyst.
  • alumina carrier 140 ml water and 5 ml nitric acid (the content of which is 60%) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and then calcinated at 560° C. for 4 hours. 100 g calcinated carrier is impregnated with a solution formed by dissolving 16.7 g magnesium nitrate and 3 g strontium nitrate into water, dried in air at 120° C., and calcinated at 1050° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • 10 g nickel nitrate is added to 20 ml water with stirring. While stirring, 2.1 g cerium nitrate and 0.3 g ammonium molybdate are added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 400° C. for 4 hours, thereby obtaining the catalyst.
  • alumina carrier 140 ml water, 5 ml nitric acid (the content of which is 60%) and 14 ml silica sol (comprising 40% silica) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and then calcinated at 460° C. for 4 hours. 100 g calcinated carrier is impregnated with a solution formed by dissolving 20 g magnesium nitrate and 3.5 g strontium nitrate into water, dried in air at 120° C., and calcinated at 1000° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • nickel nitrate 8.6 g nickel nitrate is added to 20 ml water with stirring. While stirring, 1.5 g lanthanum nitrate and 0.6 g ammonium tungstate are added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 350° C. for 4 hours, thereby obtaining the catalyst.
  • alumina carrier 140 ml water, 5 ml nitric acid (the content of which is 60%) and 14 ml silica sol (comprising 40% silica) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and calcinated at 1000° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • nickel nitrate 8.6 g nickel nitrate is added to 20 ml water with stirring. While stirring, 1.5 g lanthanum nitrate and 0.6 g ammonium tungstate are added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 350° C. for 4 hours, thereby obtaining the catalyst.
  • alumina carrier 140 ml water, 5 ml nitric acid (the content of which is 60%) and 9 ml silica sol (comprising 40% silica) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and then calcinated at 460° C. for 4 hours. 100 g calcinated carrier is impregnated with a solution formed by dissolving 15.5 g magnesium nitrate into water, dried in air at 120° C., and calcinated at 1030° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • nickel nitrate is added to 20 ml water with stirring. While stirring, 0.63 g cerium nitrate, 0.62 g lanthanum nitrate and 0.5 g ammonium tungstate are added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 400° C. for 4 hours, thereby obtaining the catalyst.
  • the formed alumina carrier is dried in air at 120° C., and calcinated at 1030° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • nickel nitrate 7.9 g nickel nitrate is added to 20 ml water with stirring. While stirring, 0.6 g ammonium molybdate is added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 400° C. for 4 hours, thereby obtaining the catalyst.
  • alumina carrier 140 ml water, 5 ml nitric acid (the content of which is 60%) and 12 ml silica sol (comprising 40% silica) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and then calcinated at 460° C. for 4 hours. 100 g calcinated carrier is impregnated with a solution formed by dissolving 5.8 g strontium nitrate into water, dried in air at 120° C., and calcinated at 1020° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • nickel nitrate is added to 20 ml water with stirring. While stirring, 1.1 g cerium nitrate, 1.1 g lanthanum nitrate and 0.6 g potassium chromate are added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 350° C. for 4 hours, thereby obtaining the catalyst.
  • alumina carrier 140 ml water, 5 ml nitric acid (the content of which is 60%) and 12 ml silica sol (comprising 40% silica) are added to 300 g pseudo-boehmite alumina powder. After kneading and extruding, the formed alumina carrier is dried in air at 120° C., and then calcinated at 460° C. for 4 hours. 100 g calcinated carrier is impregnated with a solution formed by dissolving 21.6 g magnesium nitrate into wate, dried in air at 120° C., and calcinated at 1020° C. for 4 hours, thereby obtaining the Al 2 O 3 carrier.
  • nickel nitrate is added to 20 ml water with stirring. While stirring, 1.1 g cerium nitrate is added. The pH of the solution is adjusted to 4. Then 10 g carrier is impregnated with the solution, aged for 12 hours, dried at 120° C., and calcinated at 350° C. for 4 hours, thereby obtaining the catalyst.
  • Iodine value measured according to IC1 method, expressed in g I 2 /100 g oil;
  • Diolefin measured according to maleic anhydride method, expressed in g I 2 /100 g oil;
  • Arsenic content measured by DV-4300 atomic emission spectroscopy
  • Sulfur content measured by WK-2B microcoulometric detector
  • Colloid measured according to Petroleum Product Testing Method SYB-2103-60.
  • the full distillate pyrolysis gasoline is used as the starting materials, the properties of which are shown in Table 1.
  • the catalysts of Examples 1, 2, 3 and 4 as well as Comparative Examples 1, 2, 3 and 4 are evaluated on 100 ml adiabatic bed hydrogenation apparatus. Firstly, the catalyst is reduced under hydrogen at the temperature of 350-400° C. for 10 hours. The temperature is lowered to 60° C. After the catalyst is inactivated by cyclohexane containing 1000 ppm dimethyl disulfide for 2 hours, the raw oil is added.
  • Intake temperature room temperature ⁇ 60° C.
  • Air speed of fresh raw oil 3.5h ⁇ 1 ,
  • the volume ratio of hydrogen to oil 200:1 (based on the fresh oil).
  • the evaluation is carried out for 200 hours. And the iodine value and diolefin of the products are analyzed every 6 hours. The average data of the iodine value and diolefin of the product for each catalyst during the 200-hour evaluation are shown in Table 2.
  • Example 2 1000-hour long period evaluation is performed on the catalyst of Example 2. The evaluation was carried out on 100 ml adiabatic bed hydrogenation apparatus. Firstly, the catalyst is reduced under hydrogen at the temperature of 400-450° C. for 10 hours. The temperature is lowered to 60° C. After the catalyst is inactivated by cyclohexane containing 1000 ppm dimethyl disulfide for 3 hours, the raw oil is added.
  • Intake temperature room temperature ⁇ 70° C.
  • Air speed of fresh raw oil 2.8h ⁇ 1 ,
  • the volume ratio of hydrogen to oil 200:1 (based on the fresh oil).
  • the iodine value and diolefin of the product are analyzed every 12 hours. The average data during every 200 hours are taken.
  • the indexes of hydrogenation raw oil (C 5 -C 9 ) are shown in Table 3.
  • the hydrogenation catalyst according to the present invention has good hydrogenation performance, especially has impurity and colloid resistance as well as good hydrogenation stability.
  • the catalyst can be applied to selective hydrogenation of diolefin unsaturated hydrocarbons, especially the first-stage selective hydrogenation process of full distillate pyrolysis gasoline.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US12/741,017 2007-11-01 2008-10-22 selective nickel based hydrogenation catalyst and the preparation thereof Abandoned US20100298129A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
CN200710176670A CN101423775B (zh) 2007-11-01 2007-11-01 一种选择性镍系加氢催化剂及其制备方法
CN200710176670.9 2007-11-01
PCT/CN2008/001781 WO2009062386A1 (en) 2007-11-01 2008-10-22 A selective nickle based htdrogenation catalyst and the preparation thereof

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2008/001781 A-371-Of-International WO2009062386A1 (en) 2007-11-01 2008-10-22 A selective nickle based htdrogenation catalyst and the preparation thereof

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US14/456,858 Division US9597668B2 (en) 2007-11-01 2014-08-11 Selective nickel based hydrogenation catalyst and the preparation thereof

Publications (1)

Publication Number Publication Date
US20100298129A1 true US20100298129A1 (en) 2010-11-25

Family

ID=40614658

Family Applications (2)

Application Number Title Priority Date Filing Date
US12/741,017 Abandoned US20100298129A1 (en) 2007-11-01 2008-10-22 selective nickel based hydrogenation catalyst and the preparation thereof
US14/456,858 Active 2029-06-07 US9597668B2 (en) 2007-11-01 2014-08-11 Selective nickel based hydrogenation catalyst and the preparation thereof

Family Applications After (1)

Application Number Title Priority Date Filing Date
US14/456,858 Active 2029-06-07 US9597668B2 (en) 2007-11-01 2014-08-11 Selective nickel based hydrogenation catalyst and the preparation thereof

Country Status (7)

Country Link
US (2) US20100298129A1 (ja)
JP (1) JP5357170B2 (ja)
KR (1) KR101469303B1 (ja)
CN (1) CN101423775B (ja)
GB (1) GB2467086B8 (ja)
MY (1) MY150048A (ja)
WO (1) WO2009062386A1 (ja)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102139218A (zh) * 2011-03-22 2011-08-03 中国华能集团清洁能源技术研究院有限公司 一种煤制合成气完全甲烷化的催化剂及其制备方法
CN102259004A (zh) * 2011-07-06 2011-11-30 中国华能集团清洁能源技术研究院有限公司 用于煤制天然气甲烷化反应器的催化剂及其制备方法
CN102259005A (zh) * 2011-07-06 2011-11-30 中国华能集团清洁能源技术研究院有限公司 用于煤制天然气辅助甲烷化反应器的催化剂及其制备方法
US9518229B2 (en) 2012-07-20 2016-12-13 Inaeris Technologies, Llc Catalysts for thermo-catalytic conversion of biomass, and methods of making and using
US9522392B2 (en) 2013-03-15 2016-12-20 Inaeris Technologies, Llc Phosphorous promotion of zeolite-containing catalysts
CN111054364A (zh) * 2018-10-16 2020-04-24 中国石油化工股份有限公司 一种镍系烷基化原料选择加氢催化剂及其制备方法
CN112569954A (zh) * 2020-12-09 2021-03-30 山东京博石油化工有限公司 一种炼厂干气脱炔催化剂、其制备方法和应用
CN114082421A (zh) * 2021-10-26 2022-02-25 北京化工大学 加氢催化剂及其制备方法以及在异辛烯醛加氢中的应用
CN114289028A (zh) * 2021-12-01 2022-04-08 中国海洋石油集团有限公司 一种顺酐液相连续加氢制备丁二酸酐的非贵金属催化剂及其制备方法
CN114433103A (zh) * 2020-11-03 2022-05-06 中国石油化工股份有限公司 一种选择性制备辛醛或辛烯醇的催化剂及其制备方法和应用

Families Citing this family (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102574114B (zh) * 2009-04-22 2015-12-02 科伊奥股份有限公司 活性受控的热解催化剂
JP2011083701A (ja) * 2009-10-15 2011-04-28 Jx Nippon Oil & Energy Corp 水素源不純物に対する抗被毒特性に優れた水添触媒及びその製造方法
CN102614889B (zh) * 2011-01-31 2014-06-04 北京安耐吉能源工程技术有限公司 一种加氢处理催化剂及其应用
CN102641740A (zh) * 2011-02-22 2012-08-22 中国石油天然气股份有限公司 一种双烯选择性加氢催化剂及制备方法
CN102989477B (zh) * 2011-09-09 2015-02-25 中国石油天然气股份有限公司 一种镍基加氢催化剂、制备方法和催化剂的还原、再生方法
CN102994144B (zh) * 2011-09-09 2015-05-13 中国石油天然气股份有限公司 一种石油烃类裂解碳四、碳五馏分饱和加氢方法
CN102994143B (zh) * 2011-09-09 2015-01-07 中国石油天然气股份有限公司 石油烃类裂解碳四、碳五馏分饱和加氢方法
CN102994145B (zh) * 2011-09-09 2014-11-26 中国石油天然气股份有限公司 石油烃类裂解碳九馏分饱和加氢方法
KR101268831B1 (ko) 2011-10-07 2013-05-29 한국화학연구원 선택적 고리 열림 반응용 니켈 담지 촉매
CN104109081B (zh) * 2013-04-16 2016-04-06 中国石油化工股份有限公司 提高合成气制乙二醇产品质量的方法
CN104248983B (zh) * 2013-06-28 2016-12-28 中国石油天然气股份有限公司 一种SiO2-Al2O3 复合载体的制备方法
CN105983413B (zh) * 2015-01-30 2018-12-25 中国石油天然气股份有限公司 高活性渣油加氢催化剂的制备方法
CN108865241B (zh) * 2017-05-15 2021-01-01 中国石油天然气股份有限公司 一种裂解汽油碳八馏分选择加氢方法
CN107057757B (zh) * 2017-06-02 2018-10-02 钦州学院 一种裂解汽油一段选择性加氢的方法
CN110237846A (zh) * 2018-03-09 2019-09-17 中国石油化工股份有限公司 一种镍系催化剂及其制备方法和应用
CN112469502A (zh) * 2018-08-08 2021-03-09 格雷斯公司 催化剂、其制备方法和选择性氢化方法
US20220023836A1 (en) * 2018-12-21 2022-01-27 Jgc Catalysts And Chemicals Ltd. Metal trapping, method for manufacturing metal trapping, and fluid catalytic cracking catalyst
KR20200086983A (ko) * 2019-01-10 2020-07-20 코아텍주식회사 대용량 과불화화합물 제거를 위한 금속산화물 촉매 및 그 제조 방법
CN110102277B (zh) * 2019-05-20 2021-12-14 浙江恒澜科技有限公司 再生蒽醌降解物的催化剂及其制备方法和再生蒽醌降解物的方法
CN112661620A (zh) * 2019-10-16 2021-04-16 中国石油化工股份有限公司 一种环戊酮的制备方法
EP3822332A1 (en) 2019-11-13 2021-05-19 Indian Oil Corporation Limited Catalyst for selective hydrogenation of diolefins and method for preparing catalyst
CN111905745B (zh) * 2020-08-06 2022-01-04 中国科学院过程工程研究所 一种用于丙烯酸甲酯加氢反应的镍基催化剂及其方法
KR20220097688A (ko) * 2020-12-30 2022-07-08 한화솔루션 주식회사 내황성이 향상된 수소화 반응용 촉매 및 이의 제조방법
CN112675865B (zh) * 2021-01-06 2022-02-11 中国地质大学（武汉） 一种高活性、高稳定性担载镍催化剂及其制备方法和应用
CN114950470B (zh) * 2022-06-30 2023-07-25 东营科尔特新材料有限公司 镍基催化剂及其制备方法和在丙烯中丙炔及丙二烯选择性加氢中的应用

Citations (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3472763A (en) * 1965-02-13 1969-10-14 Inst Francais Du Petrole Catalytic hydrogenation of diolefins
US3635841A (en) * 1969-06-16 1972-01-18 Engelhard Min & Chem Novel anthraquinone hydrogenation catalyst
US4469816A (en) * 1982-12-14 1984-09-04 Allied Corporation Palladium on alumina aerogel catalyst composition and process for making same
US4499205A (en) * 1982-04-12 1985-02-12 Nissan Motor Company, Limited High activity catalyst for reforming of methanol and process of preparing same
US5258558A (en) * 1991-10-21 1993-11-02 Uop Direct conversion of butyraldehyde to 2-ethylhexanol-1
US5648576A (en) * 1994-06-09 1997-07-15 Institut Francais Du Petrole Catalytic hydrogenation process and a catalyst for use in the process
US6054409A (en) * 1995-06-06 2000-04-25 Institut Francais Du Petrole Selective hydrogenation catalyst and a process using that catalyst
US6268522B1 (en) * 1997-06-05 2001-07-31 Celanese Gmbh Catalyst, process for its production and its use for preparing vinyl acetate
US6350717B1 (en) * 1998-09-04 2002-02-26 Basf Aktiengesellschaft Catalyst and process for the selective hydrogenation of unsaturated compounds in hydrocarbon streams
US6509292B1 (en) * 2001-03-30 2003-01-21 Sud-Chemie Inc. Process for selective hydrogenation of acetylene in an ethylene purification process
US6518213B1 (en) * 1999-08-06 2003-02-11 Nissan Motor Co., Ltd. Exhaust gas purifying catalyst and process for preparing the catalyst
US6528453B2 (en) * 2000-07-26 2003-03-04 Bp Chemicals Limited Process for making a catalyst composition
US6797669B2 (en) * 2000-12-29 2004-09-28 China Petroleum & Chemical Corporation Catalyst for selective hydrogenation, its preparation process and application
US6822127B2 (en) * 2000-09-29 2004-11-23 China Petroleum & Chemical Corporation Selective hydrogenation catalyst for selectively hydrogenating of unsaturated olefin, process for preparing the same and its use
US6821922B1 (en) * 1998-09-24 2004-11-23 Degussa - Huls Ag Supported catalyst for the production of vinyl acetate monomer
US6936568B2 (en) * 2002-06-12 2005-08-30 Sud-Chemie Inc. Selective hydrogenation catalyst
US20060030482A1 (en) * 2003-08-04 2006-02-09 Catalytic Distillation Technologies Ni hydrogenation catalysts, manufacture and use
US20060178262A1 (en) * 2005-01-20 2006-08-10 Andrzej Rokicki Hydrogenation catalyst
US20060217679A1 (en) * 1998-09-28 2006-09-28 Hanly Kevin B Intravenous drug access system
US7247760B2 (en) * 2002-06-14 2007-07-24 Chevron Phillips Chemical Company Hydrogenation palladium-silver catalyst and methods
WO2008040175A1 (fr) * 2006-09-20 2008-04-10 China Petroleum & Chemical Corporation Catalyseur au nickel pour hydrogénation sélective
US7521393B2 (en) * 2004-07-27 2009-04-21 Süd-Chemie Inc Selective hydrogenation catalyst designed for raw gas feed streams
US7902104B2 (en) * 2004-06-23 2011-03-08 Arkema France Divided solid composition composed of grains provided with continuous metal deposition, method for the production and use thereof in the form of a catalyst
US8067334B2 (en) * 2004-10-13 2011-11-29 Basf Se Selective hydrogenation catalyst

Family Cites Families (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3615207A (en) 1969-06-16 1971-10-26 Fmc Corp Production of hydrogen peroxide by anthraquinone process
US3899444A (en) 1972-02-07 1975-08-12 Ethyl Corp Exhaust gas catalyst support
JPS51104488A (en) 1975-03-13 1976-09-16 Toyota Motor Co Ltd Shokubaitantai oyobi shokubai
US4000207A (en) 1975-05-12 1976-12-28 Scm Corporation Isomerization of alpha-pinene to beta-pinene with neutralized alumina-supported mixed metal catalyst
GB1571910A (en) 1975-12-18 1980-07-23 Nat Distillers Chem Corp Vinyl acetate process and catalyst therefor
US4220559A (en) 1978-02-14 1980-09-02 Engelhard Minerals & Chemicals Corporation High temperature-stable catalyst composition
US4390456A (en) 1979-08-08 1983-06-28 W. R. Grace & Co. Spheroidal alumina particles and catalysts employing the particles as a support
US4410455A (en) 1980-10-22 1983-10-18 Imperial Chemical Industries Plc Process for producing a hydrogenation catalyst
CN85100761A (zh) 1985-04-01 1986-09-24 中国科学院山西煤炭化学研究所 纤维状双烯选择加氢催化剂及其制法
GB8620982D0 (en) 1986-08-29 1986-10-08 Shell Int Research Catalyst preparation
US4919902A (en) 1987-09-30 1990-04-24 Allied-Signal Inc. Catalyst for treatment of exhaust gases from internal combustion engines
FR2647365B1 (fr) 1989-05-24 1991-08-30 Inst Francais Du Petrole Catalyseur multifonctionnel pour le traitement des gaz d'echappement des moteurs a combustion interne, contenant de l'uranium, au moins un promoteur de l'uranium et au moins un metal precieux et sa preparation
DE19500366C1 (de) 1995-01-09 1996-05-02 Basf Ag Palladium-Trägerkatalysator und seine Verwendung
GB2298194A (en) 1995-02-24 1996-08-28 Beeson & Sons Ltd Child resistant closures for containers
CN1055107C (zh) 1997-11-28 2000-08-02 中国石油化工总公司 一种选择性加氢催化剂
US5945570A (en) * 1998-10-29 1999-08-31 Arhancet; Juan Pedro Catalyst and process for preparing 1,3-propanediol
CN1107704C (zh) 2000-02-03 2003-05-07 中国石油天然气股份有限公司兰州石化分公司 裂解汽油选择性加氢催化剂
KR100419858B1 (ko) * 2001-01-17 2004-02-25 한국화학연구원 디올레핀류 화합물의 선택적 수소화 반응을 위한 수식된니켈-알루미나계 촉매와 그 제조방법
JP2003200054A (ja) * 2001-11-05 2003-07-15 Catalysts & Chem Ind Co Ltd 炭化水素油の水素化処理触媒及びその製造方法
CN1218020C (zh) 2002-03-13 2005-09-07 中国石油化工股份有限公司 用于裂解汽油一段选择性加氢的催化剂
CN100387335C (zh) 2004-10-26 2008-05-14 福州大学 钯—氧化铝催化剂及其制备方法
CN100512955C (zh) 2005-10-31 2009-07-15 中国石油化工股份有限公司 一种炔烃及二烯烃选择加氢催化剂及其制备和应用
CN100487086C (zh) * 2006-01-06 2009-05-13 中国石油天然气股份有限公司 一种选择性镍系加氢催化剂及其制备方法、应用
CN100567461C (zh) * 2006-03-17 2009-12-09 中国石油天然气股份有限公司 一种镍系加氢催化剂及其制备方法、应用
CN101433841B (zh) 2007-12-13 2010-04-14 中国石油天然气股份有限公司 一种选择性加氢催化剂及其制备方法

Patent Citations (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3472763A (en) * 1965-02-13 1969-10-14 Inst Francais Du Petrole Catalytic hydrogenation of diolefins
US3635841A (en) * 1969-06-16 1972-01-18 Engelhard Min & Chem Novel anthraquinone hydrogenation catalyst
US4499205A (en) * 1982-04-12 1985-02-12 Nissan Motor Company, Limited High activity catalyst for reforming of methanol and process of preparing same
US4469816A (en) * 1982-12-14 1984-09-04 Allied Corporation Palladium on alumina aerogel catalyst composition and process for making same
US5258558A (en) * 1991-10-21 1993-11-02 Uop Direct conversion of butyraldehyde to 2-ethylhexanol-1
US5648576A (en) * 1994-06-09 1997-07-15 Institut Francais Du Petrole Catalytic hydrogenation process and a catalyst for use in the process
US6054409A (en) * 1995-06-06 2000-04-25 Institut Francais Du Petrole Selective hydrogenation catalyst and a process using that catalyst
US6268522B1 (en) * 1997-06-05 2001-07-31 Celanese Gmbh Catalyst, process for its production and its use for preparing vinyl acetate
US6350717B1 (en) * 1998-09-04 2002-02-26 Basf Aktiengesellschaft Catalyst and process for the selective hydrogenation of unsaturated compounds in hydrocarbon streams
US6821922B1 (en) * 1998-09-24 2004-11-23 Degussa - Huls Ag Supported catalyst for the production of vinyl acetate monomer
US20060217679A1 (en) * 1998-09-28 2006-09-28 Hanly Kevin B Intravenous drug access system
US6518213B1 (en) * 1999-08-06 2003-02-11 Nissan Motor Co., Ltd. Exhaust gas purifying catalyst and process for preparing the catalyst
US6534438B1 (en) * 2000-07-26 2003-03-18 Bp Chemicals Limited Catalyst composition
US6806382B2 (en) * 2000-07-26 2004-10-19 Michael James Baker Catalyst composition and process for making same
US6528453B2 (en) * 2000-07-26 2003-03-04 Bp Chemicals Limited Process for making a catalyst composition
US6822127B2 (en) * 2000-09-29 2004-11-23 China Petroleum & Chemical Corporation Selective hydrogenation catalyst for selectively hydrogenating of unsaturated olefin, process for preparing the same and its use
US6797669B2 (en) * 2000-12-29 2004-09-28 China Petroleum & Chemical Corporation Catalyst for selective hydrogenation, its preparation process and application
US6509292B1 (en) * 2001-03-30 2003-01-21 Sud-Chemie Inc. Process for selective hydrogenation of acetylene in an ethylene purification process
US6936568B2 (en) * 2002-06-12 2005-08-30 Sud-Chemie Inc. Selective hydrogenation catalyst
US7247760B2 (en) * 2002-06-14 2007-07-24 Chevron Phillips Chemical Company Hydrogenation palladium-silver catalyst and methods
US20060030482A1 (en) * 2003-08-04 2006-02-09 Catalytic Distillation Technologies Ni hydrogenation catalysts, manufacture and use
US7902104B2 (en) * 2004-06-23 2011-03-08 Arkema France Divided solid composition composed of grains provided with continuous metal deposition, method for the production and use thereof in the form of a catalyst
US7521393B2 (en) * 2004-07-27 2009-04-21 Süd-Chemie Inc Selective hydrogenation catalyst designed for raw gas feed streams
US8067334B2 (en) * 2004-10-13 2011-11-29 Basf Se Selective hydrogenation catalyst
US20060178262A1 (en) * 2005-01-20 2006-08-10 Andrzej Rokicki Hydrogenation catalyst
WO2008040175A1 (fr) * 2006-09-20 2008-04-10 China Petroleum & Chemical Corporation Catalyseur au nickel pour hydrogénation sélective
US8236726B2 (en) * 2006-09-20 2012-08-07 China Petroleum & Chemical Corporation Nickel catalyst for selective hydrogenation

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
CN101037613 A 9/2007, machine translation, Dong et al *
CN1995290A, 7/2007, machine translation, Liang et al *

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102139218A (zh) * 2011-03-22 2011-08-03 中国华能集团清洁能源技术研究院有限公司 一种煤制合成气完全甲烷化的催化剂及其制备方法
CN102139218B (zh) * 2011-03-22 2012-09-26 中国华能集团清洁能源技术研究院有限公司 一种煤制合成气完全甲烷化的催化剂及其制备方法
CN102259004A (zh) * 2011-07-06 2011-11-30 中国华能集团清洁能源技术研究院有限公司 用于煤制天然气甲烷化反应器的催化剂及其制备方法
CN102259005A (zh) * 2011-07-06 2011-11-30 中国华能集团清洁能源技术研究院有限公司 用于煤制天然气辅助甲烷化反应器的催化剂及其制备方法
US9518229B2 (en) 2012-07-20 2016-12-13 Inaeris Technologies, Llc Catalysts for thermo-catalytic conversion of biomass, and methods of making and using
US9522392B2 (en) 2013-03-15 2016-12-20 Inaeris Technologies, Llc Phosphorous promotion of zeolite-containing catalysts
CN111054364A (zh) * 2018-10-16 2020-04-24 中国石油化工股份有限公司 一种镍系烷基化原料选择加氢催化剂及其制备方法
CN114433103A (zh) * 2020-11-03 2022-05-06 中国石油化工股份有限公司 一种选择性制备辛醛或辛烯醇的催化剂及其制备方法和应用
CN112569954A (zh) * 2020-12-09 2021-03-30 山东京博石油化工有限公司 一种炼厂干气脱炔催化剂、其制备方法和应用
CN114082421A (zh) * 2021-10-26 2022-02-25 北京化工大学 加氢催化剂及其制备方法以及在异辛烯醛加氢中的应用
CN114289028A (zh) * 2021-12-01 2022-04-08 中国海洋石油集团有限公司 一种顺酐液相连续加氢制备丁二酸酐的非贵金属催化剂及其制备方法

Also Published As

Publication number Publication date
JP5357170B2 (ja) 2013-12-04
GB2467086B8 (en) 2012-02-15
GB201008986D0 (en) 2010-07-14
CN101423775B (zh) 2010-05-12
WO2009062386A1 (en) 2009-05-22
CN101423775A (zh) 2009-05-06
JP2011502050A (ja) 2011-01-20
MY150048A (en) 2013-11-29
US9597668B2 (en) 2017-03-21
GB2467086A (en) 2010-07-21
US20140349844A1 (en) 2014-11-27
KR101469303B1 (ko) 2014-12-04
KR20100075498A (ko) 2010-07-02
GB2467086B (en) 2012-02-08

Similar Documents

Publication Publication Date Title
US9597668B2 (en) Selective nickel based hydrogenation catalyst and the preparation thereof
US7686942B2 (en) Method for preparation of ethylene and propylene by catalytic cracking using a fluid-bed catalyst
CN100487086C (zh) 一种选择性镍系加氢催化剂及其制备方法、应用
EP3023147B1 (en) Iron-based hydrogenation catalyst and applications thereof
DE102010024904A1 (de) Form und Verfahren zu deren Herstellung und Katalysator und Verfahren zu dessen Herstellung
WO1994025154A1 (en) Dehydrogenation catalyst having improved moisture stability, and process for making and using the catalyst
US4153580A (en) CO conversion catalyst
US10661253B2 (en) Method of preparation of mixed metal oxide using glucose oxidation assisted precipitation
WO2011103698A1 (zh) 加氢精制催化剂
RU2639159C2 (ru) Катализатор, способ приготовления носителя, способ приготовления катализатора и способ гидроочистки углеводородного сырья
CN108187709B (zh) 一种深度加氢脱硫催化剂的制备方法及该催化剂的应用
RU2626397C1 (ru) Способ гидрокрекинга углеводородного сырья
WO2019080832A1 (zh) 一种分子筛组合物、其制造方法及其用途
US20180370872A1 (en) Dehydrogenation catalyst for alkylaromatic compound, process for producing same, and dehydrogenation method using same
NO327439B1 (no) Katalysator til hydrogenbehandling av dieselolje og fremgangsmate for fremstilling av katalysatoren
CN108421554B (zh) 加氢精制催化剂及其制备方法和应用
CN103418401A (zh) 丙烯氧化法制丙烯醛催化剂及其制备方法
US4490483A (en) Process for preparing catalysts
CN106475106B (zh) 一种合成气甲烷化制天然气催化剂的制备方法
RU2385764C2 (ru) Способ приготовления катализаторов для глубокой гидроочистки нефтяных фракций
RU2708643C1 (ru) Катализатор гидроочистки бензина каталитического крекинга и способ его получения
CN108654630B (zh) 一种耐硫变换催化剂及其制备方法
CN114471669B (zh) 一种加氢裂化催化剂及其制备方法和应用
WO2022078371A1 (zh) 铁-钾-铈基复合氧化物催化剂及其制备和应用
CN105363488B (zh) 一种加氢裂化催化剂及其制备和应用

Legal Events

Date Code Title Description
AS Assignment

Owner name: PETROCHINA COMPANY LIMITED, CHINA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:LIANG, SHUNQIN;QIAN, YING;LV, LONGGANG;AND OTHERS;SIGNING DATES FROM 20100605 TO 20100608;REEL/FRAME:024540/0696

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION