WO2017000427A1 - 一种催化剂及由合成气一步法直接制备低碳烯烃的方法 - Google Patents

一种催化剂及由合成气一步法直接制备低碳烯烃的方法 Download PDF

Info

Publication number
WO2017000427A1
WO2017000427A1 PCT/CN2015/092091 CN2015092091W WO2017000427A1 WO 2017000427 A1 WO2017000427 A1 WO 2017000427A1 CN 2015092091 W CN2015092091 W CN 2015092091W WO 2017000427 A1 WO2017000427 A1 WO 2017000427A1
Authority
WO
WIPO (PCT)
Prior art keywords
inorganic solid
solid acid
metal
acid
temperature
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.)
Ceased
Application number
PCT/CN2015/092091
Other languages
English (en)
French (fr)
Inventor
潘秀莲
李津京
焦峰
包信和
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.)
Dalian Institute of Chemical Physics
Original Assignee
Dalian Institute of Chemical Physics
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 Dalian Institute of Chemical Physics filed Critical Dalian Institute of Chemical Physics
Priority to EP15896956.8A priority Critical patent/EP3318327A4/en
Priority to JP2017567812A priority patent/JP6666365B2/ja
Priority to RU2018103755A priority patent/RU2706241C2/ru
Priority to US15/740,653 priority patent/US10532961B2/en
Publication of WO2017000427A1 publication Critical patent/WO2017000427A1/zh
Priority to ZA2017/08553A priority patent/ZA201708553B/en
Priority to SA517390644A priority patent/SA517390644B1/ar
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

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
    • B01J23/005—Spinels
    • 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
    • B01J23/06—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of zinc, cadmium or mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/26—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
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/32—Manganese, technetium or rhenium
    • B01J23/34—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
    • B01J23/74—Iron group metals
    • B01J23/75—Cobalt
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
    • B01J29/042—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41 containing iron group metals, noble metals or copper
    • B01J29/043—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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
    • B01J29/042—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41 containing iron group metals, noble metals or copper
    • B01J29/044—Iron group metals or copper
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
    • B01J29/045—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/405—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
    • B01J29/46—Iron group metals or copper
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7049—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B01J29/7065—CHA-type, e.g. Chabazite, LZ-218
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
    • B01J29/74—Noble metals
    • B01J29/743—CHA-type, e.g. Chabazite, LZ-218
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
    • B01J29/76—Iron group metals or copper
    • B01J29/763—CHA-type, e.g. Chabazite, LZ-218
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J29/783—CHA-type, e.g. Chabazite, LZ-218
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/82—Phosphates
    • B01J29/84—Aluminophosphates containing other elements, e.g. metals, boron
    • B01J29/85—Silicoaluminophosphates [SAPO compounds]
    • 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
    • B01J35/19—Catalysts containing parts with different compositions
    • 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
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • 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
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B01J35/45—Nanoparticles
    • 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
    • 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
    • B01J35/61—Surface area
    • B01J35/617—500-1000 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
    • 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
    • B01J35/64—Pore diameter
    • 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
    • B01J35/64—Pore diameter
    • B01J35/643—Pore diameter less than 2 nm
    • 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
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • 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
    • B01J35/64—Pore diameter
    • B01J35/651—50-500 nm
    • 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
    • B01J35/66—Pore distribution
    • B01J35/695—Pore distribution polymodal
    • 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
    • B01J35/70—Catalysts, in general, characterised by their form or physical properties characterised by their crystalline properties, e.g. semi-crystalline
    • B01J35/77—Compounds characterised by their crystallite size
    • 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
    • B01J37/0213—Preparation of the impregnating solution
    • 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
    • B01J37/03—Precipitation; Co-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
    • B01J37/16—Reducing
    • B01J37/18—Reducing with gases containing free hydrogen
    • 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
    • B01J37/34—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation
    • B01J37/341—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of electric or magnetic fields, wave energy or particle radiation
    • B01J37/343—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of electric or magnetic fields, wave energy or particle radiation of ultrasonic wave energy
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0425—Catalysts; their physical properties
    • C07C1/043—Catalysts; their physical properties characterised by the composition
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0425—Catalysts; their physical properties
    • C07C1/043—Catalysts; their physical properties characterised by the composition
    • C07C1/0435—Catalysts; their physical properties characterised by the composition containing a metal of group 8 or a compound thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/04—Ethene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/06—Propene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/08—Alkenes with four carbon atoms
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/60—Synthesis on 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/60—Synthesis on support
    • B01J2229/66—Synthesis on support on metal supports
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/396—Distribution of the active metal ingredient
    • B01J35/397—Egg shell like
    • 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
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/396—Distribution of the active metal ingredient
    • B01J35/398—Egg yolk like
    • 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
    • B01J37/009—Preparation by separation, e.g. by filtration, decantation, screening
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
    • C07C2529/74—Noble metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
    • C07C2529/76—Iron group metals or copper
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/82—Phosphates
    • C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
    • C07C2529/85—Silicoaluminophosphates (SAPO compounds)
    • 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
    • C10G2400/20—C2-C4 olefins
    • 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 invention belongs to the field of preparing low carbon olefins, and particularly relates to a method for preparing low carbon olefins by one-step synthesis gas and a catalyst thereof.
  • Low-carbon olefins including ethylene, propylene, and butene, are important raw materials for synthetic plastics, fibers, and various chemical materials. As the national economy grows, so does the consumer demand. At present, low-carbon olefins are mainly produced by the petrochemical route of naphtha cracking. With the increasing consumption of global petroleum resources and the high crude oil prices, especially for China, where oil resources are scarce, more than 60% of oil consumption per year depends on imports. 70% of the raw materials for low-carbon olefin production in China are crude oil refining. The obtained naphtha and light hydrocarbons seek an alternative process route, and the development of a method for preparing low-carbon olefins from non-oil-based carbon resources such as coal and biomass has important social and strategic significance.
  • Coal is used as raw material.
  • the synthesis gas that is, the mixture of CO and H 2
  • the synthesis gas is converted into methanol, and the methanol to olefin (MTO) process is mature and has entered industrialization.
  • the catalyst is modified molecular sieve SAPO-34 or ZSM-5, the methanol conversion rate is close to 100%, the selectivity of ethylene and propylene is 85-90%, and only a small amount of C 5+ or more long carbon chain hydrocarbons are formed.
  • the sales cost of the direct synthesis of low-carbon olefin from coal-based syngas is more advantageous. If the content of low-carbon olefins can be further increased in the total product to more than 40%, the economic advantage will be more obvious.
  • Direct conversion of synthesis gas to lower olefins can be obtained by conventional Fischer-Tropsch reaction routes.
  • the CO dissociates and adsorbs on the surface of the catalyst, undergoes hydrogenation to form a CH x intermediate species adsorbed on the surface, and then the individual carbon species undergo a polymerization reaction through surface catalytic insertion to achieve carbon chain growth, and generate different carbon numbers. Hydrocarbons.
  • the hydrocarbons are widely distributed, with a predictable C 2 -C 4 hydrocarbon selectivity of no more than 58%, and a gasoline fraction C 5 -C 11 with a maximum selectivity of 45%, while producing large amounts of methane and higher alkanes.
  • Fe-based catalysts have the advantages of low cost and easy availability, high activity and high selectivity of low-carbon olefins, and are the most promising synthetic low-carbon olefin catalysts.
  • researchers can effectively improve the selectivity of low-carbon olefins by adding additives of different compositions, such as alkali metals K, Na, and transition metals Mn, Cu, and the like.
  • Luer Chemical Company of Germany has developed a multi-component auxiliaries promoted Fe-Zn-Mn-K catalyst for the synthesis of light olefins [12].
  • the preparation method and process of the catalyst can directly affect the dispersion and size of the active component, thereby modulating the activity of the reaction and the selectivity of the product.
  • Beijing University of Chemical Technology uses a supercritical fluid combination technology (ie, chemical precipitation, gel-like, supercritical drying method) to highly disperse the active component Fe and additives, and prepare a nano-scale Fe-based catalyst.
  • the conversion of CO is greater than 96%.
  • the selectivity of low-carbon olefins in hydrocarbons is greater than 54% [Beijing University of Chemical Technology, a nano-catalyst for synthesis of low-carbon olefins by synthesis gas and preparation method: China, 101396662 [P]. 2009-04-01] .
  • the catalyst bed cracked a large amount of the C 5+ product into a lower olefin, whereby the hydrocarbon product obtained had a selectivity to low carbon hydrocarbons of 52% and the selectivity of the lower olefins to 28% of the total product.
  • the invention provides a method for directly converting synthesis gas into a low-carbon olefin and a catalyst thereof, and the hydrocarbon in the obtained hydrocarbon has a selectivity of 60 to 95, which is a hydrocarbon product containing 2 to 4 carbon atoms. %, wherein the selectivity of low carbon olefins including ethylene, propylene and butene accounts for 50-85%.
  • the present invention provides a process for directly converting a low carbon olefin from a synthesis gas by a synthesis gas and a catalyst therefor.
  • the method comprises a composite catalyst material, a raw material molecule CO in a metal composite having a defect site Surface activation, the adsorbed additional CO reacts with the oxygen atoms generated by the dissociation to form CO2. Since another raw material molecule hydrogen cannot generate water with the dissociated oxygen atoms, a large amount of high-value hydrogen is consumed, so that the reaction raw material
  • the process can directly use the mixture of the coal gasifier outlet, which can reduce the water-gas conversion section of high energy consumption;
  • the CHx intermediate formed on the surface of the composite cannot stay on the surface of the composite, desorbs into the gas phase in the form of free radicals, enters the pores of the porous material, performs chain-limited chain growth, and selects to generate target hydrocarbon molecules.
  • the one-step direct catalytic conversion of synthesis gas and the high selectivity of low-carbon olefins are achieved, which not only breaks through the limitation of the ASF distribution of the product in the conventional Fischer-Tropsch reaction path, but also obtains low-carbon olefins with high selectivity and eliminates the extra The methanol synthesis process, as well as the water gas shift process.
  • the selectivity of light olefins in hydrocarbons is as high as 50-85%, and the conversion per pass of carbon monoxide is 10-50%.
  • the method has the characteristics of simple process and low equipment investment, and it can be foreseen that the method can significantly reduce the production cost of low-carbon olefins and has important application value.
  • the catalyst is a composite material composed of a multi-component metal composite and a multi-stage pore structure inorganic solid acid;
  • the inorganic solid acid has a multi-stage pore structure of micropores, mesopores and macropores;
  • the metal complex is dispersed in the inorganic solid acid In the surface or in the tunnel;
  • the content of the multicomponent metal composite in the entire catalyst is 10 wt.% to 75 wt.%, preferably 25 wt.% to 75 wt.%, based on 100% by mass of the total mass of the catalyst;
  • the inorganic solid acid of the multi-stage pore structure is composed of inorganic solid acid secondary particles, and the inorganic solid acid secondary particles have a size of 100 nm to 500 ⁇ m, preferably 150 nm to 100 ⁇ m;
  • the inorganic solid acid secondary particles are formed by stacking inorganic solid acid crystal grains having a size of 5 to 200 nm (preferably 20 to 120 nm);
  • the inorganic solid acid secondary particles have a three-dimensional three-stage pore structure, including three pores of a first-stage pore, a second-stage pore, and a third-order pore;
  • the primary pore is a microporous pore having a pore diameter of less than 2 nm, and the microporous is located inside the inorganic solid acid crystal grain;
  • the secondary pores are mesopores having a pore diameter of 2 nm to 50 nm, preferably 2-15 nm, and the secondary pores are formed by depositing inorganic solid acid crystal grains, and are located inside the inorganic solid acid secondary particles and the pores of the tertiary pores.
  • the wall On the wall
  • the tertiary pores are large pores having a pore diameter distribution greater than 50 nm, and are formed by depositing inorganic solid acid secondary particles;
  • the three types of channels are connected to each other to form a three-dimensional three-stage channel structure, the second-level holes may be located in adjacent three-stage hole walls, and the first-level holes may be located in adjacent second-level holes and/or third-order holes. ;
  • the inorganic solid acid of the multi-stage pore structure has a BET specific surface area of 100 to 1200 m 2 /g and a pore volume of 0.25 to 0.80 ml/g as measured by N 2 physical adsorption; and the micropore accounts for 10-65 according to the specific surface area.
  • % mesopores account for 20-75%, macropores account for 15-70%; preferred micropores have a specific surface area of 10-60%, mesoporous specific surface area accounts for 20-70%, and macropores account for 20-70%;
  • the specific surface area of the micropores is 10-50%, the mesoporous specific surface area is 30-70% of the total specific surface area, and the macropores are 20-60%.
  • the metal in the multicomponent metal composite is two or more metal elements, preferably two to five metal elements;
  • the metal composite includes metal oxides and metals, metal carbides, metals One or more of a nitride, and a metal mineral acid salt;
  • the metal element includes essential metal elements as well as other elements, wherein the essential metal elements are Zn or Co or Cr or Mn;
  • the other elements are Li, Na, Mg, Al, K, Ca, Sr, Ba, Ti, V, Cr, Mn, Fe, Co, Cu, Ga, Ge, Zr, Mo.
  • Pd, Ag, Cd, In, Sn, Cs, La, and Ce other elements are preferably Al, K, Ti, V, Cr, Mn, Co, Cu, Ce, Pd
  • the other elements are more preferably one or more of Al, Ti, Cr, Mn, Co, Cu, Pd, and Ce;
  • the other elements are Li, Na, Mg, Al, K, Ca, Sr, Ba, Ti, V, Cr, Mn, Fe, Cu, Zn, Ga, Ge, Zr, Mo.
  • Pd, Ag, Cd, In, Sn, Cs, La, and Ce other elements are preferably Al, K, Ti, V, Cr, Mn, Cu, Zn, Ce, Pd
  • the other elements are more preferably one or more of Al, Ti, Cr, Mn, Cu, Zn, Pd, and Ce;
  • the other elements are Li, Na, Mg, Al, K, Ca, Sr, Ba, Ti, V, Mn, Fe, Co, Cu, Zn, Ga, Ge, Zr, Mo.
  • Pd, Ag, Cd, In, Sn, Cs, La, and Ce other elements are preferably Al, K, Ti, V, Mn, Co, Cu, Zn, Ce, Pd
  • the other elements are preferably one or more of Al, Ti, Mn, Co, Cu, Zn, Pd, and Ce;
  • the other elements are Li, Na, Mg, Al, K, Ca, Sr, Ba, Ti, Cr, Fe, Co, Cu, Zn, Ga, Ge, Zr, Mo, Pd.
  • One or more of Ag, Cd, In, Sn, Cs, La, and Ce other elements are preferably Al, K, Ti, V, Cr, Co, Cu, Zn, In, La, Mo, Ce
  • Pd Pd
  • the other elements are more preferably one or more of Al, Ti, Cr, Co, Cu, Zn, Pd, and Ce;
  • the content of the metal oxide is 5 to 90%, and the total mass content of one or more of the metal and the metal carbide and the metal nitride may be 10% or less.
  • the content of the metal mineral acid salt is 10 to 95%; preferably, the content of the metal oxide is 30 to 90%, and the total mass content of one or more of the metal and metal carbide and the metal nitride is less than 5%.
  • the content of the metal mineral acid salt is 10-70%;
  • the total molar ratio of the essential element Zn or Co or Cr or Mn to other elements in the multicomponent metal composite is (0.1 to 5.0): 1, preferably in a molar ratio of 0.2 to 3.5;
  • the inorganic acid salt is composed of a cation and an anion, wherein Li, Na, Mg, Al, K, Ca, Sr, Ba, Ti, V, Cr, Mn, Fe, Co, Cu, Zn, Ga, Ge, Zr
  • the metal composite is formed by uniformly dispersing a metal oxide according to claim 2 and one or more crystal grains of a metal, a metal carbide, a metal nitride or a metal mineral acid salt, and a crystal grain size thereof. It is 0.5-20 nm, preferably 1-10 nm; at the same time, the crystal grains are further deposited to form secondary particles having a secondary particle size of 10 nm to 200 ⁇ m, and the pores formed in the secondary particles are formed to have a pore diameter of 2-20 nm, preferably 5- 15nm.
  • the inorganic solid acid is composed of H, O as an essential element, and one or more elements of Al, Si, P, Zr, Ti, Ge, forming an inorganic solid acid composed of a silicon oxyhydrogen element, An inorganic solid acid composed of a sialon, an inorganic solid acid composed of a silicoaluminophosphorus element, an inorganic solid acid composed of a titanium silicon oxyhydrogen element, an inorganic solid acid composed of zirconium oxyhydrogen element, One or more of an inorganic solid acid composed of a silicon oxyhydrogen element and an inorganic solid acid composed of yttrium aluminum phosphide.
  • the inorganic solid acid of the multi-stage pore structure has an acidic characteristic
  • the acid sites are distributed in the three-dimensional three-level pores of claim 1;
  • the acidity is defined according to NH 3 -TPD, and the solid inorganic acid comprises three acids of weak acid, medium strong acid and strong acid;
  • TCD records the thermal conductivity signal of desorption of NH3, draws a desorption curve, and divides the inorganic solid into three acid strengths according to the apex of the peak position of the curve;
  • the weak acid is an acid site having a NH 3 desorption temperature of less than 275 ° C;
  • the medium strong acid is an acid site in which the NH 3 desorption temperature is 275-500 ° C;
  • the strong acid is an acid bit having a NH 3 desorption temperature greater than 500 ° C;
  • the inorganic solid acid, the amount of medium strong acid sites is 0.06-10 mol / kg; preferably 1-10 mol / kg;
  • the multi-stage pore structure inorganic solid acid preparation method comprises a soft template hydrothermal method, a hard template hydrothermal method or a crystallization control hydrothermal method; in a soft template hydrothermal method, a hard template hydrothermal method or a crystallization control hydrothermal method
  • the use of constant temperature stirring aging treatment is advantageous for forming an inorganic solid acid having a multi-stage pore structure
  • the mixture is stirred and dispersed, and an organic microporous template is added to prepare a liquid phase dispersion system;
  • the aging method is to control the prepared liquid phase dispersion system at a temperature of 20-60 ° C for 10 min to 24 h, and a stirring rate of 50- 1000 rpm; stirring rate during crystallization 50-500 rpm, temperature 120-250 ° C, time 12h-10day; washing method can be filter washing or centrifugal washing, filtration washing should ensure that the filtrate pH is 6.5 at the end of washing -7.5, centrifugal washing should ensure that the supernatant is 6.5-7.5 at the end of washing; the drying process, the temperature is 100-150 ° C, the time is greater than 12h; the roasting process, the temperature is 500-650 ° C, time 1-8h ;
  • the soft template hydrothermal method uses an organic mesoporous template to synthesize a multi-stage pore structure inorganic solid acid by hydrothermal method, and the specific steps involve preparation, aging, crystallization, washing, drying and roasting of a uniform sol dispersion.
  • the uniform sol dispersion is prepared by weighing the precursor of the element contained in the inorganic solid acid into a container containing water at a desired mass ratio, stirring and dispersing at room temperature, and adding the organic microporous template.
  • the agent and the organic mesoporous template agent (the mass ratio is 0.3-0.8), and the liquid phase dispersion system is prepared.
  • the temperature during the aging process is controlled at 20-60 ° C, the time is 10 min-24 h, the stirring rate is 50-1000 rpm; during the crystallization process Stirring rate 50-500 rpm, temperature 120-250 ° C, time 12h-10day; washing method can be filter washing or centrifugal washing, filter washing should ensure that the filtrate pH is 6.5-7.5 at the end of washing, centrifugal washing should ensure the supernatant at the end of washing
  • the liquid is 6.5-7.5; the drying process, the temperature is 100-150 ° C, the time is greater than 12 h; the roasting process, the temperature is 500-650 ° C, time 1-8 h;
  • the hard template hydrothermal method is a nano carbon material which can be oxidized at 650 ° C, SBA series, M41S series, HMS series, MSU series, KIT series, FDU series, AMS series, HOM series, MCM-41 mesopores
  • One or more of the molecular sieves are used as a hard template to synthesize a multi-stage pore structure inorganic solid acid by hydrothermal method, and the specific steps involve preparation, aging, crystallization, washing, drying and calcination of the uniform sol dispersion;
  • the uniform sol dispersion is prepared by weighing the precursor of the element contained in the inorganic solid acid into a container containing water at a desired mass ratio, stirring and dispersing, and adding an organic microporous template and a hard template material (they The mass ratio is 0.3-0.8) to obtain a liquid phase dispersion system, which inhibits grain growth and promotes the formation of mesopores by small grains; the temperature is controlled at 20-60 ° C
  • the precursor in the homogeneous sol dispersion is water glass, silica sol, ultrafine SiO2, white carbon black, sodium silicate, TMOS, silicate, silicon tetrachloride, kaolin, aluminum nitrate, aluminum sulfate, sodium aluminate.
  • the organic microporous templating agent is TMA, TPA, TEA, TEAOH, DDO, TBA, TQA, ethylenediamine, pyrrolidine, choline, PDN, RDN, PDA, pentaerythritol, hydroxy acid, propyl thioaldehyde, tripropylamine.
  • DABCO di-n-propylamine, tert-butylamine, isopropylamine, quinuclidine, neopentylamine, triethanolamine, dicyclohexylamine, N,N-dimethylbenzylamine, N,N-dimethylolamine, N, One or more of N-diethylethanolamine, 2-methylpyridine, piperidine, and morphine;
  • the organic mesoporous template is CTBA, CTBABr, dodecyl phosphate, long chain primary amine, polyoxyethylene, polyoxypropylene, polyoxyethylene block ether copolymer, P123, gelatin and glutaraldehyde crosslink One or more of the substances, TPHAC;
  • the composite mode of the multi-component metal composite and the multi-stage pore structure inorganic solid acid in the catalyst comprises a coating growth method, an ultrasonic assisted chemical compounding method, or a physical composite method;
  • the coating growth method is characterized in that a multi-component metal composite is grown on the surface of the multi-component metal composite by at least 80% coverage or completely covered by the method of claim 6.
  • the inorganic solid acid of the grade pore structure, that is, the uniform sol dispersion is prepared first, and then the multi-component metal composite is dispersed in the uniform sol dispersion, and then subjected to aging, crystallization, washing, drying and roasting to obtain a multi-stage coating.
  • Multi-component metal composite of inorganic solid acid with pore structure multi-component metal composite consisting of Mg, Al, Ca, Sr, Ba, Ti, V, Cr, Mn, Fe, Co, Cu, Zn, Zr
  • Metal oxides and inorganic acid salts composed of elements of Mo, Pd, Ag, Cd, In, Sn, La, and Ce are prepared by coprecipitation, impregnation, or ultrasonic ion exchange
  • Li, Na, K, Ga, Metal oxides and inorganic acid salts composed of Ge and Cs elements are prepared by impregnation method or ultrasonic ion exchange method
  • Al, Fe, Co, Cu, Zn, Mo, Pd elements can also be prepared by chemical vapor deposition or impregnation;
  • the ultrasonic assisted chemical compounding method is obtained by introducing a multi-component metal composite by ultrasonic coprecipitation, chemical vapor deposition or ultrasonic ion exchange on an inorganic solid acid of a multi-stage pore structure;
  • the physical compounding method is to compound a multi-stage pore structure inorganic solid acid and a multi-component metal composite by ball milling, mechanical mixing, shaking, and oscillating mixing mechanochemistry.
  • roasting drying temperature is 80-150 ° C, time is greater than 12h, roasting The temperature is 300-650 ° C, time 1-3h;
  • the metal precursor is selected from one or more of a nitrate, a formate, an acetate, a halide, a carbonyl compound, and a C1-C5 organic acid salt; and the precipitant is selected from the group consisting of carbonic acid
  • the precipitant is selected from the group consisting of carbonic acid
  • One or more of ammonium, ammonium hydrogencarbonate, lithium carbonate, lithium hydrogencarbonate, sodium carbonate, sodium hydrogencarbonate, potassium carbonate, potassium hydrogencarbonate, magnesium carbonate or oxalic acid preferably ammonium carbonate, ammonium hydrogencarbonate, carbonic acid Sodium hydrogencarbonate, potassium hydrogencarbonate, preferably ammonium carbonate, ammonium hydrogencarbonate, sodium hydrogencarbonate; precipitation temperature controlled in the range of 2 ⁇ 80 ° C, drying temperature of 80 ⁇ 150 ° C, time greater than 12h, roasting temperature of 300 ⁇ 650 ° C, time 1-3h, the roasting atmosphere can be flowing air or standing air;
  • the ultrasonic ion exchange method refers to dissolving two or more metal precursors required for a multi-component metal complex in a solvent to obtain two or more metal cation solutions, and then multi-stage pore structure.
  • Inorganic solid The acid is added to the above solution under ultrasonic agitation.
  • the ultrasonic method may be bath ultrasound or Tip ultrasound, the ultrasonic power is 1-20 W/(ml sample), the frequency is 40 KHz-80 MHz, the precipitation temperature is 2 ° C-60 ° C, and the time is 1 h- 12h, stirring rate 50-500rpm, and then washed, dried, calcined, the washing method can be filtration washing or centrifugal washing, so that the pH after washing is 6.5-7.5, the drying temperature is 80-150 ° C, the time is more than 12h, the baking temperature is 300-650 ° C, time 1-3h;
  • the ball milling method in the physical compounding has a temperature of 25 to 100 ° C, and the carrier gas is: a) nitrogen and/or an inert gas, b) a mixture of hydrogen and nitrogen and/or an inert gas, wherein the hydrogen is in the mixed gas. a volume of 5 to 50%, c) a mixture of CO and nitrogen and/or an inert gas, wherein the volume of CO in the mixture is 5 to 20%, or d) a mixture of O 2 and nitrogen and/or an inert gas , wherein the volume of O 2 in the mixed gas is 5-20%, and the inert gas is one or more of helium, argon, and helium;
  • the mechanical mixing method in the physical compounding refers to a multi-component metal composite and a multi-stage pore structure using a mixing device including a 3D rotary mixer, a planetary mixer, or a turbo mixer.
  • the inorganic solid acid is added into the container, and one or more of the pressing force, the impact force, the cutting force and the friction force generated by the high-speed movement of the material and the container are used to achieve separation, crushing, mixing, etc.
  • the modulation temperature and the carrier gas atmosphere realize the conversion of mechanical energy, thermal energy and chemical energy, and further enhance the interaction between different components; during the reaction, the temperature is set at 20-100 ° C, and the carrier gas atmosphere is: a) nitrogen and/or inert a gas, b) a mixture of hydrogen and nitrogen and/or an inert gas, wherein the volume of hydrogen in the mixture is 5 to 50%, c) a mixture of CO and nitrogen and/or an inert gas, wherein the CO is in the mixture a volume of 5 to 20%, d) a mixture of O 2 and nitrogen and/or an inert gas, wherein the volume of O 2 in the mixed gas is 5-20%, and the inert gas is helium, argon, helium One or more of the gases.
  • the catalytic reaction is carried out by using any of the catalysts, and the H 2 /CO volume ratio of the reaction raw material gas is 0.5/1 to 4/1 at a desired reaction temperature and reaction pressure to prepare a C2-C4 lower olefin, that is, two
  • the olefin having from one carbon atom to four carbon atoms includes one or more of ethylene, propylene and butene.
  • the catalytic reaction before the reaction, comprises a catalyst pretreatment process, the pretreatment atmosphere is a) a mixture of H 2 and CO, wherein the H 2 /CO volume ratio is 0.5 / 1 ⁇ 4 / 1;
  • a mixture of CO and an inert gas in c), the volume percentage of CO in the mixed gas is 5 to 100%, and the inert gas is one or both of nitrogen, helium, argon or helium. the above;
  • the pretreatment temperature of the catalyst is 250-600 ° C, the pretreatment pressure is 0.1-3.0 MPa, the pre-treatment space velocity is 500-5000 h -1 , and the space velocity is preferably 1000-4000 h -1 ;
  • the pore size and acidity of the inorganic solid acid can modulate the selectivity of the lower hydrocarbons and the relative proportion of the olefins and alkanes therein.
  • the reaction raw material gas is a mixed gas, the mixed gas contains H 2 , CO, and other gases, and the other gases are one or two of an inert gas and/or a non-inert gas;
  • the inert gas is one or more of nitrogen, helium, argon and helium, and the volume content in the reaction raw material gas is less than 10%;
  • the non-inert gas is one or both of carbon dioxide, vaporized water, methanol, and ethanol, and the volume content in the reaction raw material gas is less than 50%.
  • the device used in the reaction is a fluidized bed, a moving bed or a fixed bed;
  • the reaction temperature is 300-500 ° C, the reaction temperature is preferably 350-450 ° C, the space velocity is 500-10000 h -1 , and the space velocity is preferably 2000-7000 h -1 ;
  • the reaction is a continuous flow reaction mode or a batch reaction mode
  • the reaction pressure is 0.1 to 6.0 MPa, and the reaction pressure is preferably 1.0 to 5.0 MPa;
  • the reaction pressure is 1.0 to 10 MPa, and the reaction pressure is preferably 1.0 to 5.0 MPa.
  • the present invention relates to a process for the direct conversion of a low-carbon olefin from a synthesis gas in a one-step process, the low-carbon olefin product comprising two or more of ethylene, propylene and butene; the content of the low-carbon olefin product in all hydrocarbons It is 50 to 85%.
  • the one-step process for producing low-carbon olefins has the following characteristics:
  • the product differs from the Anderson Schultz Flory distribution law controlled by chain growth; in the conventional Fischer-Tropsch reaction product, the predictable C 2 -C 4 hydrocarbon selectivity is up to 58%, while the present invention provides C 2 -C 4 in the product.
  • the selectivity can reach 60-95%;
  • the selectivity of the low carbon olefin in the total hydrocarbon product is as high as 50-85%;
  • the catalyst is different from the traditional Fetato reaction to produce transition metals such as Fe, Co and the like as components of low-carbon hydrocarbons, but a composite catalytic material of inorganic solid acid and multi-component metal composite containing multi-stage pore structure. .
  • the invention and the two-stage process which has been industrialized at present, that is, the process of converting synthesis gas into methanol or dimethyl ether and then converting methanol or dimethyl ether into low-carbon olefin, has the following characteristics:
  • One reactor, one catalyst, one-step conversion can significantly reduce equipment investment and production costs
  • the catalyst is a catalytic material composed of a composite solid acid containing a multi-stage pore structure and a multi-component metal composite, and the product selectivity can be well regulated;
  • the catalyst has good stability and long life.
  • the invention has the advantages of single operation unit, good process repeatability, high product selectivity and long catalyst life (>500h), and has broad industrial application prospects.
  • the catalyst used in the present invention has the following advantages: In the synthesis of a low-carbon olefin in the synthesis gas, the catalyst provided by the present invention is a composite material obtained by compounding a multi-component metal composite with a multi-stage pore structure inorganic solid acid.
  • the catalyst is different from the catalyst of the transition metal as the main component used in the conventional Fischer-Tropsch reaction to produce low carbon hydrocarbons, and is also different from the catalyst used in the methanol synthesis by the industrial two-stage method.
  • the innovations include structure and function: the structure is at the same time as the catalyst A multi-stage pore structure with micropores and mesopores.
  • This unique structure gives the catalyst a significant advantage of long-term operation (>500h) under the reaction conditions without deactivation; the functional aspect is that it can directly catalyze the synthesis gas conversion. There is no need to support a high-energy water-gas shift process, no need to convert syngas to methanol and extract methanol, and it is different from the traditional chain growth mechanism.
  • One step can produce low-carbon hydrocarbon products with a selectivity of 60-95%.
  • the Anderson-Schultz-Flory distribution limit in the conventional Fischer-Tropsch reaction, and the selectivity of methane and long carbon chain products (C5 + ) is less than 5-10%.
  • Figure 1 is an SEM image of Cr 1 Zn 1 @SiAl of the core-shell structure of Example 8;
  • Figure 2 is an XRD pattern of Cu 1 Zn 1 @SiAl in Example 8.
  • Example 3 is a N 2 physical adsorption curve and a pore size distribution diagram of a silicon phosphorus aluminum inorganic solid acid having a multistage pore structure in Example 14;
  • the continuous flow fixed bed reaction is exemplified, but the catalyst is also suitable for use in a fluidized bed reactor.
  • the device is equipped with a gas mass flow meter, a gas deoxidation dehydration tube and an on-line product analysis chromatograph (the exhaust gas of the reactor is directly connected to the chromatographic quantitative valve for periodic real-time sampling analysis).
  • the above catalysts are uniformly sieved to 20-40 mesh particles or 40-60 mesh for use.
  • a CuZnAl multi-component metal composite, a silico-alumina inorganic solid acid having a multi-stage pore structure is exemplified.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a specific pore surface ratio of 347 m 2 /g and a pore size distribution.
  • the mesopore specific surface area was 214 m 2 /g
  • the macropore specific surface was 62 m 2 /g
  • the mesoporous pore size was distributed at 2-15 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal complex contained CuO, ZnO, Al2O3, ZnAlO2 and a silica-alumina inorganic solid acid with CHA structure.
  • the grain size of the metal oxide was 5-15 nm; inorganic solid acid crystal grains The size of 40-70nm; scanning electron microscopy (SEM) characterization shows that the multi-stage pore structure of silicon-aluminum inorganic solid acid secondary particles is 10-100 ⁇ m, inorganic solid acid crystal size is 10-100nm; high-resolution transmission electron microscope (HRTEM) The characterization shows that the multi-component metal complex has a grain size of 5-15 nm and a secondary particle size of 15-50 nm; the medium-strong acid corresponds to a NH3 desorption peak temperature of 360 ° C, and the medium-strong acid site has a molar amount of 2 mol/kg.
  • the medium strong acid is defined by NH 3 -TPD and is based on the position of the desorption peak of NH3.
  • the medium strong acid is an acid site in which the NH 3 desorption temperature is 275-500 °C.
  • the preparation process is basically the same as that in the first embodiment. The difference is that in the preparation process of the silicon-aluminum inorganic solid acid of the multi-stage pore structure in the first embodiment, the crystallization temperature is changed to 150 ° C for 5 days to prepare a medium strong acid site. The amount is a silica-alumina inorganic solid acid of a structure of 0.8 mol/kg.
  • the preparation process was substantially the same as that in Example 1, except that in the preparation process of the silicoalumino inorganic solid acid of the multistage pore structure in Example 1, the crystallization temperature was 140 ° C for 3 days, and the preparation was carried out.
  • the amount of the strong acid site was 0.01 mol/kg of a silica-alumina inorganic solid acid.
  • Example 2 the preparation process was substantially the same as that of Example 1, except that in the preparation process of the silicoalumino inorganic solid acid of the multistage pore structure in Example 1, the crystallization temperature was 140 ° C, 22 h, and a medium strong acid was prepared. The amount of the sites was 0.005 mol/kg of a silica-alumina inorganic solid acid.
  • reaction results are shown in the following table under the reaction conditions of 365 ° C, 2 MPa volumetric space velocity 4000 h -1 .
  • the conversion rate in Comparative Example 1, 2 is extremely low, because the medium acidity in the solid acid is small, and the intermediate species produced on the multi-component metal complex cannot be converted into the target product in time and well.
  • the selectivity of methane is greatly increased, exceeding 30%, and the selectivity of low-carbon olefins is also reduced.
  • the catalyst of the present invention containing more moderately strong acid has a greatly improved conversion rate and a high selectivity for the target product olefin.
  • the conversion of Example 1 was significantly higher than the conversion of Example 2 because the catalyst was within the preferred range. It can be seen that the acid content of the silica-alumina inorganic solid acid of the multi-stage pore structure is extremely important for the regulation of catalytic properties including conversion and selectivity.
  • the water bath was quenched to room temperature, and the washing was repeated by centrifugation so that the pH of the supernatant was 7 at the end of the washing, and the precipitate was dried at 130 ° C for 17 h, and then at 580 ° C.
  • the silicon-phosphorus aluminum inorganic solid acid having a multi-stage pore structure was obtained by calcination in the gas for 5 hours.
  • the physical adsorption and desorption of nitrogen showed that the catalyst has a multi-stage pore structure and the pore size distribution is
  • the mesopores have a pore size distribution of 2-8 nm and a total specific surface area of 416 m 2 /g, wherein the mesoporous specific surface area accounts for 35% of the total specific surface area, and the macroporous surface area accounts for 20% of the total area.
  • the multicomponent metal composite comprises a silica-alumina inorganic solid acid containing Cr2O3, CrO3, ZnO, Al2O3, ZnCr2O4, and CHA structures, a metal oxide grain size of 7-16 nm, and an inorganic solid acid grain size of 50-60 nm; Scanning electron microscopy (SEM) characterization showed that the secondary particle size of the silicon-aluminum inorganic solid acid was 100-500 ⁇ m.
  • the high-resolution transmission electron microscopy (HRTEM) characterization showed that the grain size of the multi-component metal complex was 7-16 nm, and the secondary particle size.
  • the temperature of the NH3 desorption peak corresponding to the medium strong acid is 386 ° C, and the amount of the strong acid site is 6 mol / kg.
  • the preparation process is basically the same as that of the embodiment 3. The difference is that when the silicon-aluminum inorganic solid acid is prepared, the stirring time is changed to 3 h, the crystallization time is changed to 24 h, and the total specific surface area is 377 m 2 /g, and the mesoporous specific surface area is prepared.
  • the structure is 21% of the total specific surface area, and the macroporous specific surface area accounts for 20% of the total specific surface area of the CHA-structured silico-alumina inorganic solid acid; the medium-strong acid corresponds to the NH3 desorption peak temperature of 385 ° C, and the medium-strong acid site is 5.8 mol. /kg.
  • the preparation process was basically the same as that in Example 3, except that when the silicon-aluminum inorganic solid acid was prepared, the aging temperature was changed to 80 ° C, and after stirring for 2 days, it was crystallized at 240 ° C for 24 hours to obtain a total specific surface area. 232m 2 /g, mesoporous specific surface area accounts for 4% of the total specific surface area, macroporous specific surface area accounts for 1% of the total specific surface area, CHA structure silico-alumina inorganic solid acid; medium-strong acid corresponding NH3 desorption peak temperature is 411 ° C The amount of the medium strong acid site is 2 mol/kg.
  • the preparation process was basically the same as that in Example 3, except that when the silicon-aluminum inorganic solid acid was prepared, the aging temperature was changed to 30 ° C, and after stirring for 2 days, it was crystallized at 240 ° C for 48 hours to obtain a total specific surface area. 287 m 2 /g, the mesoporous specific surface area accounts for 10% of the total specific surface area, and the macroporous specific surface area accounts for 4% of the total specific surface area of the CHA-structured silico-alumina inorganic solid acid; the medium-strong acid corresponds to the NH3 desorption peak temperature of 390 ° C, The amount of medium strong acid sites is 5 mol/kg.
  • the preparation process was substantially the same as that of Comparative Example 3 except that the preparation of the silica-alumina inorganic solid acid was carried out according to the specific surface area, using a commercial SBA-15 molecular sieve having a mesoporous distribution at 4-8 nm and Comparative Example 3
  • the silicon-aluminum inorganic solid acid is mechanically mixed, and the mixing ratio is 13:7 according to the specific surface area of the silicon-aluminum inorganic solid acid and SBA-15, and then ground and mixed to obtain a silica-alumina inorganic solid acid having a mesoporous and microporous composite, wherein
  • the pores account for 62% of the total specific surface area
  • the mesoporous specific surface area accounts for 36% of the total specific surface area
  • the macropores account for 2% of the total specific surface area.
  • the mesoporous channels having a diameter of 2 nm to 50 nm are not formed by the accumulation of inorganic solid acid crystal grains, wherein the first-order pores are not located in the adjacent second-order pores and/or the tertiary-order pore walls, but the first-order pores exist in isolation.
  • the second-order three-level holes exist in isolation, and the three types of holes that do not meet the requirements are connected to each other, and do not constitute a three-dimensional multi-stage channel structure.
  • reaction results are as shown in the following table under the reaction conditions of 400 ° C and a volume velocity of 2.5 MPa of 4000 hr -1 .
  • the selectivity of the lower olefins in Example 3 was significantly better than that in Comparatives 3 and 4, while the selectivity in Example 3 was better than in Example 4 due to the medium silicon aluminum in the catalyst of Example 3.
  • the mesoporous specific surface area of the inorganic solid acid accounts for 35% of the total specific surface area, and the surface area of the macropores accounts for 20% of the total area.
  • the specific surface area accounts for 21% of the total specific surface area
  • the specific surface area of the macropores accounts for the total specific surface area. 20%, in a more preferred range, so that the mass transfer is better, the hydrogenation to produce alkanes is suppressed, and the selectivity is greatly improved.
  • the selectivity of the low-carbon olefin in the comparative example is much lower than that of the catalyst of the present invention, because the molecular sieve has too few mesopores and macropores, and does not reach the content of mesopores and macropores as claimed in the claims, which is not conducive to mass transfer.
  • the change in acid strength also causes the product to be excessively hydrogenated to produce alkanes, which greatly reduces the selectivity of the lower olefins.
  • Comparative Example 5 Although the content of mesopores and macropores is in combination with the range described in the claims, the three types of pores contained therein are not directly connected to each other, and do not constitute the three-dimensional three-stage pore structure described in the claims, and SBA- In the surface of 15 itself and its pores, there is little medium strong acid, so the medium strong acid in Comparative Example 5 is mainly distributed in the micropores, rather than uniformly distributed in the three-dimensional tertiary pores, which does not meet the requirements of claim 5, so There was no substantial change compared to Comparative Example 3, and the selectivity of the lower olefins was still very low.
  • the specific surface area of mesopores accounts for 20-75%, and the macropores account for 20-65% of the catalysts that constitute the three-dimensional multi-stage pore structure.
  • the selectivity of olefins exceeds 60%, which is not only much higher than that of Comparative Examples 3, 4. It is also 58% higher than the theoretical selectivity of the conventional Fischer-Tropsch synthesis of lower olefins. It can be seen that the pore structure of the inorganic acid is extremely important for the regulation of product selectivity.
  • the method comprises the following steps: mechanical mixing of different materials by ball milling, mechanical mixing, shaker, shaking mixing and the like method.
  • a silicon-phosphorus aluminum inorganic solid acid having a multi-stage pore structure a crosslinked product of triethylamine, gelatin and glutaraldehyde is used as a template.
  • 10 g of aluminum isopropoxide, 5.30 g of concentrated phosphoric acid, 3.67 g of silica sol (containing 30% by mass), 1.46 g of triethylamine, 13.2 g of H 2 O were mixed, stirred at room temperature for 3 h, stirring speed was 400 rpm, and then 1.68 g was added. 2 wt% gelatin solution, warmed to 57 ° C, and continued to stir for 0.5 h.
  • the obtained mixture was poured into a Petri dish and frozen at 0 ° C for 12 h to obtain a jelly.
  • An appropriate amount of 5 wt% glutaraldehyde was added for crosslinking reaction, and the suspension after the reaction was centrifuged at 10,000 rpm to obtain a solid sample of 50. After drying in an oven at °C overnight, it is placed in a PTFE lining, and the small lining is placed in a large PTFE lining. The large lining needs to be pre-charged with triethylamine and water.
  • the mixed solution was then placed in a stainless steel auto-calculating crystallization tank and crystallized by dry gelation at 200 ° C for 36 h.
  • the supernatant was repeatedly washed to make the supernatant pH 7 at the end of the washing, and the precipitate was baked at 90 ° C for 6 h. After drying at 110 ° C for 12 h, it was calcined in air at 550 ° C for 3 h to obtain a silicon-phosphorus aluminum inorganic solid acid having a multi-stage pore structure.
  • the ratio of 6:0.2:1:1:1 is 17.33g of zinc nitrate hexahydrate, copper nitrate hexahydrate, cobalt nitrate hexahydrate, and chromium nitrate nonahydrate.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a specific pore surface area of 243 m 2 /g and a pore size distribution of The mesopore specific surface area was 318 m 2 /g, the macropore specific surface was 182 m 2 /g, and the mesoporous pore size was distributed at 15-25 nm.
  • the NH3 desorption peak temperature corresponding to the medium strong acid is 367 ° C, and the amount of the medium strong acid site is 1.5 mol / kg.
  • Example 6 the preparation process was substantially the same as that of Example 5, except that the content of the multicomponent metal composite was adjusted to 15 wt.% based on 100% of the total mass of the catalyst.
  • Example 6 the preparation process was substantially the same as that of Example 5, except that the content of the multicomponent metal composite was adjusted to 5 wt.% based on 100% of the total mass of the catalyst.
  • Example 7 the preparation process was substantially the same as that of Example 5 except that the content of the multicomponent metal composite was adjusted to 90 wt.% based on 100% of the total mass of the catalyst.
  • the preparation process was basically the same as that of Example 5 except that the preparation of the silicon phosphorus aluminum inorganic solid acid in the multi-stage pore structure was changed to a crystallization temperature of 190 ° C, a time of 33 h, a calcination temperature of 600 ° C, and a time of 3 h.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a mesoporous pore size distribution of 10-15 nm. Scanning electron microscopy (SEM) was used to characterize the surface.
  • the secondary particle size of the silicon-aluminum inorganic solid acid was 10-70 ⁇ m, the inorganic solid acid crystal size was 60-80 nm, and the NH3 desorption peak temperature of the medium strong acid was 385 ° C.
  • the amount is 1.5 mol/kg.
  • the preparation process was basically the same as that of Example 7, except that the preparation of the silicon phosphorus aluminum inorganic solid acid in the multi-stage pore structure was changed to a crystallization temperature of 160 ° C, a time of 24 h, a calcination temperature of 550 ° C, and a time of 8 h. Roasting is carried out under flowing air. The physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a mesoporous pore size distribution of 2-5 nm. Scanning electron microscopy (SEM) was used to characterize the surface. The secondary particle size of silicon-aluminum inorganic solid acid was 5-100 nm. XRD showed inorganic acid crystal size of 1-5 nm. The strong desorption peak of NH3 was 349 °C. The amount of the site was 0.06 mol/kg.
  • SEM scanning electron microscopy
  • the grain size of the silicon-phosphorus aluminum inorganic solid acid of the multi-stage pore structure in Examples 6 and 7, and the size of the secondary particles and the size of the mesoporous pores are all in the scope of the claims, but are implemented relative to Example 6.
  • the grain size, secondary particle size and mesoporous channel of Example 7 were in the preferred range, so that they exhibited better conversion and selectivity, while in Comparative Example 8, because they did not meet the scope of the claims, they were expressed as inorganic solid acid.
  • the degree of crystallization is not good, and thus the catalytic conversion is not well performed, so the conversion rate and selectivity are significantly worse. Therefore, the grain size of the inorganic solid acid and the size of the secondary particles and the size of the mesoporous channels are all critical for the catalytic conversion and product selectivity.
  • a multi-component metal composite-multistage pore structure inorganic solid acid composite catalyst prepared by a coating growth method.
  • the method relates to obtaining an inorganic solid acid material having one or a part of a multi-stage pore structure by hydrothermal or the like on the obtained multi-metal composite.
  • the method is not limited to bimetal, and is applicable to other metals, and can change the relative proportion of different metals.
  • Ammonia water, ammonium carbonate or ammonium hydrogencarbonate can be used as a precipitating agent.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a microporous surface area of 311 m 2 /g and a pore size distribution of
  • the mesoporous specific surface area was 203 m 2 /g
  • the surface ratio to macropores was 171 m 2 /g
  • the mesoporous pore size was distributed at 13-30 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal complex contained CuO, ZnO and a silico-alumina inorganic solid acid with MFI structure.
  • the metal oxide grain size was 8-20 nm
  • the inorganic solid acid crystal size was 55-70 nm.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a specific pore surface area of 297 m 2 /g and a pore size distribution.
  • the mesopore specific surface area is 122 m 2 /g
  • the macropore specific surface is 111 m 2 /g
  • the mesoporous pore size is distributed at 2-8 nm.
  • X-ray diffraction (XRD) characterization shows that the multi-component metal complex contains a silica-alumina inorganic solid acid of Co3O4, Co2O3, ZnO, Al2O3, ZnCo2O4 and CHA structures, and the metal oxide has a grain size of 9-17 nm.
  • the size of the film is 50-60nm.
  • Scanning electron microscopy (SEM) characterization shows that the secondary particle size of the silicon-aluminum inorganic solid acid is 100-500 ⁇ m.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal complex is 9- 17 nm, the secondary particle size is 20-100 nm; the NH3 desorption peak temperature corresponding to the medium strong acid is 363 ° C, and the amount of the medium strong acid site is 0.6 mol/kg.
  • the preparation process was basically the same as that of Example 8, except that in the process of synthesizing the multi-metal composite, no ultrasonic treatment was used, the aging was performed at 90 ° C for 0.5 h, and the calcination temperature was changed to 300 ° C, so that the final catalyst could not be used. A good crystal form is formed, resulting in a final grain size of ⁇ 1 nm.
  • the baking time was controlled to 1.5 h during the coating of the inorganic solid acid.
  • the final catalyst has a micropore ratio of 148 m 2 /g, and the pore size of the pores is distributed.
  • the mesopore specific surface area is 27 m 2 /g
  • the macropore specific surface is 7 m 2 /g
  • the mesoporous pore size is distributed between 20 and 47 nm.
  • the metal oxide grain size is ⁇ 1 nm
  • the secondary particle size is 10 nm-50 ⁇ m
  • the inorganic solid acid crystal grain size is 53-79 nm
  • the inorganic solid acid secondary particle size is 300-600 ⁇ m
  • the medium strong acid corresponding NH3 desorption peak temperature is At 410 ° C, the amount of medium strong acid sites was 0.05 mol/kg.
  • the preparation process was basically the same as that of Example 8, except that during the synthesis of the multi-metal composite, the ultrasonic treatment power was 0.5 W, the aging at 30 ° C for 3 days, and the calcination temperature was changed to 800 ° C, so that the final catalyst
  • the grain size is >30 nm.
  • the final catalyst has a micropore ratio of 757 m2/g, and the pore size of the pores is distributed.
  • the mesopore specific surface area was 147 m 2 /g
  • the macropore specific surface was 150 m 2 /g
  • the mesoporous pore size was distributed at 8-14 nm.
  • Example 8 Comparative Example 9 and Comparative Example 10, under the reaction conditions of 370 ° C, 2 MPa volumetric space velocity 7000 h -1 , the reaction results are shown in the following table.
  • Example 9 Under the reaction conditions of 400 ° C, 2.5 MPa volumetric space velocity 4000 h -1 , the reaction results are shown in the following table.
  • the grain size of the multi-component metal composite of Comparative Example 9 is very small, many of which are even in the form of clusters formed by single atoms or a small number of atoms, and the particle size is smaller than the preferred range described in the claims and smaller than that of the claims. Particle size range, Comparative Example 9 Reaction Results Although the conversion rate was increased, the methane selectivity was greatly increased by more than 30%, while the low-carbon olefin selectivity was reduced to less than 20%.
  • the grain size of the multi-metal composite is larger than the upper limit of the grain size range described in the claims, the particles are too large, and the specific surface area is decreased, resulting in insufficient activation of the synthesis gas, and the conversion rate is very low, and Hydrogen is more serious and the selectivity of low-carbon olefins is also reduced. Therefore, the grain size of the metal complex is critical for regulating the catalytic performance.
  • the preparation process and method are basically the same as those in the embodiment 5, except that the preparation process of the multi-metal composite is: weigh 17.33g of zinc nitrate hexahydrate, 0.17g of cobalt nitrate hexahydrate, 22.1g of titanium chloride, dissolved in 300ml.
  • 60.5 g of ammonium carbonate was weighed and dissolved in 300 ml of deionized water.
  • the two groups of solutions were simultaneously added dropwise to a 70 ° C thermostatically stirred deionized water for coprecipitation with an ultrasonic power of 5 W and a stirring rate of 500 rpm.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a microporous surface area of 251 m2/g and a pore size distribution at The mesopore specific surface area was 213 m 2 /g, the macropore specific surface was 216 m 2 /g, and the mesoporous pore size was distributed at 4-13 nm.
  • X-ray diffraction (XRD) characterization shows that the multi-component metal complex contains ZnO, Co3O4, TiO2, ZnCo2O4 and a silico-alumina inorganic solid acid with a CHA structure.
  • the grain size of the metal oxide is 8-20 nm, and the inorganic solid acid crystal grains The size is 60-80nm; the surface is characterized by scanning electron microscopy (SEM).
  • the secondary particle size of the silicon-aluminum inorganic solid acid is 300-700 ⁇ m.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal complex is 8- 20 nm, the secondary particle size is 30-120 nm; the NH3 desorption peak temperature corresponding to the medium strong acid is 377 ° C, and the amount of the medium strong acid site is 2 mol/kg.
  • the preparation process was basically the same as that in Example 10, except that when the metal precursor was weighed, the ratio of the metal element in the multi-metal composite was changed to Zn0.05Co3Ti2, and the metal precursor solution was synthesized according to the ratio. .
  • XRD characterization showed that the multicomponent metal complex contained ZnO, CoO, Co, ZnCo2O4, CoTiO3, and the metal Co content reached 30% in all metal atoms by atomic number, exceeding the 10% stated in the claims.
  • the multicomponent metal composite has a grain size of 8 to 40 nm and a secondary particle size of 30 to 120 nm.
  • reaction results are shown in the following table under the reaction conditions of 400 ° C, 2 MPa volumetric space velocity 6000 h -1 .
  • the preparation process and method are basically the same as those in the embodiment 8, except that the obtained multi-stage pore structure of the silicon-phosphorus aluminum inorganic solid acid is stirred at a mass ratio of 1:500 to 10% ammonium nitrate solution at 80 ° C for 8 hours, followed by suction filtration. After drying at room temperature, the mixture was stirred at 80 ° C for 8 hours at a mass ratio of 1:500 to 1% copper nitrate aqueous solution, then filtered by suction and dried at room temperature, then placed in an oven at 110 ° C for 14 h, and then calcined at 500 ° C for 1 h to obtain Cu. Multi-metal complex after ion exchange.
  • the preparation process of the multi-component metal composite differs in that the metal precursor is prepared by weighing 5.95 g of zinc nitrate hexahydrate, and ammonium molybdate is weighed according to an elemental molar ratio of 1:1, and dissolved in 100 ml of deionized water. 11 g of ammonium carbonate was weighed and dissolved in 100 ml of deionized water.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a microporous surface area of 239 m 2 /g and a pore size distribution.
  • the mesopore specific surface area was 271 m 2 /g
  • the surface ratio to macropores was 198 m 2 /g
  • the mesoporous pore size was distributed at 4-13 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal complex contained ZnO, CuO, MoO3, ZnMoO4 and a silica-alumina inorganic solid acid with a CHA structure.
  • the grain size of the metal oxide was 12-26 nm, and the inorganic solid acid crystallites.
  • the size is 60-90nm; the surface is characterized by scanning electron microscopy (SEM).
  • SEM scanning electron microscopy
  • the size of the silicon-aluminum inorganic solid acid secondary particles is 300-700 ⁇ m.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal complex is 12- 26 nm, the secondary particle size is 30-120 nm; the NH3 desorption peak temperature corresponding to the medium strong acid is 345 ° C, and the amount of the medium strong acid site is 0.5 mol/kg.
  • the preparation process is basically the same as that of the embodiment 11, except that the metal element in the multi-metal composite is replaced.
  • the metal is guaranteed to be equal to the number of atoms of the replaced metal, and the ammonium molybdate is replaced with vanadium nitrate when the metal precursor solution is disposed.
  • the preparation process is basically the same as that in the embodiment 11, except that the metal element in the multi-metal composite is replaced, the number of atoms of the replacement metal and the metal to be replaced is equal, and the ammonium molybdate is replaced with the metal precursor solution.
  • Manganese nitrate is replaced with the metal precursor solution.
  • Example 11 The difference between Example 11 and Examples 12, 13 is that the metal element composition in the multi-metal composite is changed, from Mo to V to Mn. The selectivity of the lower olefins is then gradually increased. This is preferably in accordance with the metal elements described in the claims.
  • the precipitate was dried at 110 ° C for 17 h, and then calcined in air at 550 ° C for 3 h to obtain a silico-alumina inorganic solid acid having a multi-stage pore structure.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a microporous surface area of 239 m 2 /g and a pore size distribution.
  • the mesopore specific surface area was 308 m 2 /g
  • the surface ratio to macropores was 161 m 2 /g
  • the mesoporous pore size was distributed at 4-13 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal complex contained ZnO, PdO, ZrO2, ZnZr2O4 and a silica-alumina inorganic solid acid with a CHA structure.
  • the grain size of the metal oxide was 12-22 nm, and the inorganic solid acid crystallites.
  • the size is 60-90nm; the surface is characterized by scanning electron microscopy (SEM).
  • the size of the silicon-aluminum inorganic solid acid secondary particles is 300-700 ⁇ m.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal complex is 12- 22 nm, secondary particle size 40-120 nm; medium strong acid corresponding NH3 desorption peak temperature is 370 ° C, the amount of medium strong acid sites is 1.6 mol / kg.
  • the preparation process was basically the same as that of Example 14, except that the atomic ratio of the metal element Zn to other elements in the preparation process of the metal precursor of the multi-metal composite was changed to 5:1 when the metal precursor solution was disposed.
  • Example 12 the preparation process was basically the same as that of Example 14, except that the atomic ratio of the metal element Zn to other elements in the preparation process of the metal precursor of the multi-metal composite was changed when the metal precursor solution was disposed. :1.
  • Example 14 and Comparative Example 12 changed the ratio of Zn to other elements, and the ratio of Comparative Example 12 was not in the range of the claims, so the conversion of CO was very low, while Example 15 was within the scope of the claims but was not preferred. The conversion rate is also low within the range.
  • the preparation process and method of the silicon phosphorus aluminum inorganic solid acid of the multi-stage pore structure are basically the same as those of the third embodiment, except that the obtained multi-stage pore silicon phosphorus aluminum inorganic solid acid is placed in the ampoules and connected to 10 -2 Pa or more.
  • the silicon-phosphorus aluminum inorganic solid acid of the multi-stage pore is heated, heated at 5 ° C / min to 420 ° C for 12 h, and then sealed and transferred to a glove box of Ar atmosphere, and the multi-stage pore silicon aluminum phosphate
  • the inorganic solid acid and molybdenum chloride are placed on both sides of the quartz ampoule at a mass ratio of 1:0.1.
  • the quartz ampoule After being connected to a vacuum of 10 -2 pa again, the quartz ampoule is sealed and treated to make the multi-stage pore silicon-phosphorus aluminum inorganic solid acid.
  • the ampoules of silicon-phosphorus aluminum inorganic solid acid and molybdenum chloride sealed in a multi-stage pore are placed in a tube furnace, and the temperature is raised to 400 ° C for 24 hours at 10 ° C / min, and then lowered to room temperature to break the ampule to obtain oxidation.
  • Mo-SiAlP with a molybdenum loading of 1%.
  • the preparation process of the multi-component metal composite and the composite manner of the two are basically the same as those in the embodiment 5.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a specific pore surface area of 533 m 2 /g and a pore size distribution.
  • the mesopore specific surface area was 133 m 2 /g
  • the macropore specific surface was 118 m 2 /g
  • the mesoporous pore size was distributed at 3-8 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal complex contained a silica-alumina inorganic solid acid with MoO2, ZnO, Al2O3, ZnAl2O4 and CHA structures.
  • the metal oxide grain size was 7-12 nm, and the inorganic solid acid grain size was 50-60nm; scanning electron microscopy (SEM) characterization showed that the secondary particle size of silicon-aluminum inorganic solid acid was 100-500 ⁇ m; high-resolution transmission electron microscopy (HRTEM) characterization showed that the grain size of multi-component metal complex was 7-12nm.
  • the secondary particle size is 20-100 nm; the neutral strong acid corresponds to a NH3 desorption peak temperature of 344 ° C, and the medium strong acid site is 2 mol/kg.
  • the preparation process is basically the same as that of the embodiment 16, except that the metal element in the multi-metal composite is replaced, and the number of atoms of the replacement metal and the metal to be replaced is equal, and the metal precursor solution is disposed.
  • the zinc nitrate is replaced by cerium nitrate.
  • the preparation process is basically the same as that of the embodiment 16, except that the metal element in the multi-metal composite is replaced, and the number of atoms of the replacement metal and the metal to be replaced is equal, and the metal precursor solution is disposed.
  • the zinc nitrate is replaced by a nano titanium dioxide sol.
  • reaction results are shown in the following table under the reaction conditions of 400 ° C, 3 MPa volumetric space velocity 4000 h -1 .
  • Comparative Examples 13, 14 did not contain the essential elements of the claims, so there was almost no catalytic activity.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a specific pore surface area of 289 m 2 /g and a pore size distribution of The mesopore specific surface area was 267 m 2 /g, the macropore specific surface was 161 m 2 /g, and the mesoporous pore size was distributed at 5-13 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal composites contained ZnO, Ga2O3, and TiO2 in a Cu-alumina inorganic solid acid with a CHA structure.
  • the grain size of the metal oxide was 13-20 nm, and the inorganic solid acid grain size was 60.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a micropore specific surface of 316 m 2 /g and a pore size distribution.
  • the mesopore specific surface area is 140 m 2 /g
  • the macropore specific surface is 99 m 2 /g
  • the mesoporous pore size is distributed at 3-9 nm.
  • X-ray diffraction (XRD) characterization shows that the multicomponent metal complex contains a silica-alumina inorganic solid acid of Co2O3, Co 3 O 4 , MnO 2 , TiO 2 , ZnCo 2 O 4 , ZnMnO 3 and CHA structures, and a metal oxide crystal.
  • the grain size is 9-18nm, and the inorganic solid acid grain size is 50-60nm.
  • Scanning electron microscopy (SEM) characterization shows that the secondary particle size of the silicon-aluminum inorganic solid acid is 100-500 ⁇ m.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that The grain size of the component metal complex is 9-18 nm, the secondary particle size is 20-100 nm; the NH3 desorption peak temperature corresponding to the medium strong acid is 368 ° C, and the amount of the medium strong acid site is 2.3 mol/kg.
  • Example 19 the catalyst of Example 17 was subjected to a reaction condition of 400 ° C and a volume velocity of 3.5 MPa at a space velocity of 1500 h -1 .
  • the results of the reaction as Example 19 are shown in the following table.
  • Example 20 the catalyst of Example 18 was subjected to a reaction condition of 400 ° C and a volume velocity of 3.5 MPa at a space velocity of 1500 h -1 .
  • the results of the reaction as Example 20 are shown in the following table.
  • Comparative Example 15 the catalyst of Example 17 was subjected to a reaction condition of 400 ° C and a space velocity of 3.5 MPa at a space velocity of 300 h -1 .
  • the results of the reaction as Comparative Example 15 are shown in the following table.
  • Comparative Example 16 the catalyst of Example 18 was subjected to a reaction condition of 400 ° C, a volume velocity of 3.5 MPa, and a space velocity of 300 h -1 .
  • the results of the reaction as Comparative Example 16 are shown in the following table.
  • Examples 17-20 and Comparative Examples 15-16 except that the catalyst was not changed, only the reaction space velocity conditions were changed, wherein the space velocity of Examples 17-18 was within the preferred range of the claims, so that the highest was exhibited.
  • the selectivity of the lower olefins, while the space velocities of Examples 19-20 are not within the preferred range, but fall within the scope of the claims so that there is still a higher selectivity for the lower olefins, while the relative comparative examples 15- 16, because its reaction space velocity is not within the scope of the claims, so the selectivity of low carbon olefins is very low.
  • a CaMnAl multi-component metal composite, a silico-alumina inorganic solid acid having a multi-stage pore structure is exemplified.
  • the physical adsorption and desorption of nitrogen showed that the catalyst had a multi-stage pore structure with a total specific surface area of 565 m 2 /g, wherein the microporous surface accounted for 27% of the total specific surface area, and the pore size distribution was The specific surface area of mesopores accounts for 57% of the total specific surface area, the surface area of macropores accounts for 16% of the total specific surface area, and the pore size of mesopores ranges from 6 to 12 nm.
  • X-ray diffraction (XRD) characterization showed that the multi-component metal complex contained CaO, MnO2, Al2O3, and a silica-alumina inorganic solid acid with a CHA structure.
  • the grain size of the metal oxide was 5-13 nm; the inorganic solid acid grain size It is 40-70nm; scanning electron microscopy (SEM) characterization shows that the multi-stage pore structure of silicon-aluminum inorganic solid acid secondary particles is 10-100 ⁇ m, inorganic solid acid crystal size is 10-100nm; high resolution transmission electron microscope (HRTEM) The characterization shows that the multi-component metal complex has a grain size of 5-13 nm and a secondary particle size of 15-50 nm; the medium-strong acid corresponds to a NH3 desorption peak temperature of 370 ° C, and the medium-strong acid site has a molecular weight of 6 mol/kg.
  • the preparation process of the catalyst is basically the same as that in the embodiment 21, except that in the process of preparing the silico-alumina inorganic solid acid of the multi-stage pore structure, after the precursor is weighed and mixed at room temperature, the stirring time is controlled to be 18 h, and then transferred to the hydrothermal kettle. Crystallization at 170 ° C for 5 days.
  • the obtained multi-stage pore catalyst has a total specific surface area of 493 m 2 /g, wherein the micropore ratio surface accounts for 24% of the total specific surface area, and the pore diameter distribution is The specific surface area of mesopores accounts for 53% of the total specific surface area, the surface area of macropores accounts for 23% of the total specific surface area, and the pore size of mesopores ranges from 5 to 11 nm.
  • the NH3 desorption peak temperature corresponding to the medium strong acid was 392 ° C, and the amount of the medium strong acid site was 3.1 mol/kg.
  • the preparation process of the catalyst is basically the same as that in the embodiment 21. The difference is that in the process of preparing the silico-alumina inorganic solid acid of the multi-stage pore structure, after the precursor is weighed and mixed at room temperature, the controlled control stirring time is 3 hours and then transferred to the hydrothermal kettle. Crystallization at 165 ° C for 5 days and 10 hours. Finally, it was baked at 620 ° C for 80 min.
  • the obtained multi-stage pore catalyst has a total specific surface area of 408 m 2 /g, wherein the micropore ratio surface accounts for 16% of the total specific surface area, and the pore diameter is distributed in The specific surface area of mesopores accounts for 53% of the total specific surface area, the surface area of macropores accounts for 31% of the total specific surface area, and the pore size of mesopores ranges from 5 to 13 nm.
  • the NH3 desorption peak temperature corresponding to the medium strong acid is 389 ° C, and the amount of the medium strong acid site is 3.4 mol/kg.
  • the preparation process of the catalyst is basically the same as that in the embodiment 21. The difference is that in the process of preparing the silicon-aluminum inorganic solid acid having a multi-stage pore structure, after the precursor is weighed and mixed at room temperature, the stirring temperature is controlled to control the stirring temperature for 90 hours and then transferred to the water heat. In the kettle, it was crystallized at 215 ° C for 7 days. Finally, it was baked at 550 ° C for 4 h.
  • the obtained multi-stage pore catalyst has a total specific surface area of 390 m 2 /g, wherein the micropore ratio surface accounts for 66% of the total specific surface area, and the pore diameter is distributed in The specific surface area of mesopores accounts for 26% of the total specific surface area, the surface area of macropores accounts for 8% of the total specific surface area, and the pore size of mesopores is 2-4 nm.
  • the NH3 desorption peak temperature corresponding to the medium strong acid was 403 ° C, and the amount of the medium strong acid site was 4.1 mol/kg.
  • the preparation process of the catalyst is basically the same as that in the embodiment 21. The difference is that in the process of preparing the silico-alumina inorganic solid acid of the multi-stage pore structure, after the precursor is weighed and mixed at room temperature, the controlled stirring temperature is controlled for 30 hours and then transferred to the water heat. In the kettle, it was crystallized at 175 ° C for 8 days. Finally, it was baked at 550 ° C for 3 h.
  • the obtained multi-stage pore catalyst has a total specific surface area of 314 m 2 /g, wherein the micropore specific surface accounts for 81% of the total specific surface area, and the pore diameter is distributed in The specific surface area of mesopores accounts for 14% of the total specific surface area, the surface area of macropores accounts for 5% of the total specific surface area, and the pore size of mesopores is 2-4 nm.
  • the NH3 desorption peak temperature corresponding to the medium strong acid was 368 ° C, and the amount of the medium strong acid site was 0.9 mol/kg.
  • Examples 21-23 showed superior selectivity to lower olefins as compared to Comparative Examples 17-18 because the tertiary channel content distribution in Comparative Examples 17-18 did not meet the scope of the claims, while Example 22 23 has a higher selectivity to lower olefins than Example 21, since the macropore content of Example 21 is not in the preferred range, and the tertiary pore contents of Examples 22-23 are more preferred in the preferred range. The range is so excellent.
  • the water bath was quenched to room temperature, and the centrifugal washing was repeated so that the pH of the supernatant was 7 at the end of the washing, and the precipitate was dried at 110 ° C for 24 hours, and then calcined in air at 600 ° C for 3 hours to obtain a multi-stage pore structure of silicon phosphorus aluminum inorganic solid acid. .
  • Chromium nitrate nonahydrate dissolved in aqueous solution to form a mixture A, wherein the mass ratio of inorganic solid acid to Cr is 2:1, weigh 6.3g ammonium carbonate, dissolved in 100ml water to form solution B, and solution B at 50 °C Adding 7W power tip ultrasound, stirring mixture A at 400 rpm, centrifugal washing so that the supernatant pH is 7 at the end of washing and drying in air at 110 ° C, calcined in static air at 500 ° C for 1 h to obtain Ca 0.2 Mn 2 Cr 1 /MgSiPAl.
  • the physical adsorption and desorption of nitrogen showed that the catalyst has a multi-stage pore structure and the pore size distribution is
  • the mesopores have a pore size distribution of 4-8 nm, a total specific surface area of 416 m 2 /g, wherein the micropore specific surface area accounts for 57%, the mesoporous specific surface area accounts for 21% of the total specific surface area, and the macroporous surface area accounts for 22% of the total area.
  • the secondary particle size of the silicon-aluminum inorganic solid acid is 100-500 ⁇ m, and the grain size is 5-70 nm.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal composite is 0.5-16 nm, twice.
  • the particle size is 10-100 nm, and the NH3 desorption peak temperature corresponding to the medium strong acid is 371 ° C, and the amount of the medium strong acid site is 2.1 mol/kg.
  • the preparation process of the catalyst is basically the same as that of the embodiment 21, except that in the process of preparing the silicon-aluminum inorganic solid acid having a multi-stage pore structure, the precursor is mixed and stirred at room temperature, and the stirring temperature is controlled at 40 ° C for 2 hours and then transferred to water. In a hot kettle, it was crystallized at 180 ° C for 2 days. Finally, it was baked at 550 ° C for 4 h under flowing air.
  • the physical adsorption and desorption of nitrogen showed that the catalyst has a multi-stage pore structure and the pore size distribution is
  • the mesopores have a pore size distribution of 5-9 nm, a total specific surface area of 357 m 2 /g, wherein the micropore specific surface area accounts for 43%, the mesoporous specific surface area accounts for 30% of the total specific surface area, and the macroporous surface area accounts for 27% of the total area.
  • the secondary particle size of the silicon-aluminum inorganic solid acid is 50-150 ⁇ m, and the grain size is 20-80 nm.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal complex is 1-13 nm, twice.
  • the particle size is 10-80 nm; the NH3 desorption peak temperature corresponding to the medium strong acid is 358 ° C, and the amount of the medium strong acid site is 1.9 mol/kg.
  • the preparation process of the catalyst is basically the same as that in the embodiment 21, except that in the process of preparing the silicon-aluminum inorganic solid acid having a multi-stage pore structure, after the precursor is mixed and mixed at room temperature, the stirring temperature is controlled to be 50 ° C, and the time is 1 h and then transferred to In a hydrothermal kettle, it was crystallized at 165 ° C for 5 days and 10 hours. Finally, it was baked at 620 ° C for 2 h in static air.
  • the physical adsorption and desorption of nitrogen showed that the catalyst has a multi-stage pore structure and the pore size distribution is
  • the mesopores have a pore size distribution of 4-9 nm, a total specific surface area of 4415 m 2 /g, wherein the micropore specific surface area accounts for 33%, the mesoporous specific surface area accounts for 35% of the total specific surface area, and the macroporous surface area accounts for 32% of the total area.
  • the secondary particle size of the silicon-aluminum inorganic solid acid is 50-100 ⁇ m, and the grain size is 40-90 nm.
  • the high-resolution transmission electron microscopy (HRTEM) characterization indicates that the grain size of the multi-component metal complex is 3-6 nm, twice.
  • the particle size is 10-90 nm; the NH3 desorption peak temperature corresponding to the medium strong acid is 397 ° C, and the amount of the medium strong acid site is 2.7 mol/kg.
  • the preparation process of the catalyst is basically the same as that of the embodiment 21, except that in the process of preparing the silicon-aluminum inorganic solid acid having a multi-stage pore structure, the oxide is MgO: SiO2: Al2O3: H3PO4: R: H2O: 2: 18: 16:32. : 10:150 (mass ratio), weigh the raw materials and weigh the precursor at room temperature.
  • the crystallization temperature was controlled to be 150 ° C for 24 h.
  • the physical adsorption and desorption of nitrogen showed that the catalyst has a multi-stage pore structure and the pore size distribution is
  • the mesoporous pore size is distributed at 4-9 nm, and the total specific surface area is 95 m 2 /g, wherein the micropore specific surface area accounts for 11%, the mesoporous specific surface area accounts for 55% of the total specific surface area, and the macroporous surface area accounts for 34% of the total area.
  • the NH3 desorption peak temperature corresponding to the medium strong acid is 320 ° C, and the amount of the medium strong acid site is 0.02 mol/kg.
  • the preparation process of the catalyst is basically the same as that of the embodiment 21, except that in the process of preparing the silicon-aluminum inorganic solid acid having a multi-stage pore structure, the oxide is MgO: SiO2: Al2O3: H3PO4: R: H2O: 2: 18: 16:32. : 80: 150 (mass ratio), weigh the raw materials and weigh the precursor at room temperature.
  • the crystallization temperature was controlled to be 180 ° C for 72 h.
  • the calcination temperature was controlled at 550 ° C in static air for 30 min.
  • the physical adsorption and desorption of nitrogen showed that the catalyst has a multi-stage pore structure and the pore size distribution is
  • the mesopores have a pore size distribution of 4-9 nm and a total specific surface area of 69 m 2 /g, wherein the specific pore surface area accounts for 14%, the mesoporous specific surface area accounts for 24% of the total specific surface area, and the macroporous surface area accounts for 62% of the total area.
  • the NH3 desorption peak temperature corresponding to the medium strong acid is 329 ° C, and the amount of the medium strong acid site is 0.03 mol / kg.
  • the catalysts of Examples 24-26, the size of the grains and secondary particles of the multicomponent metal composite and the silica-alumina inorganic solid acid satisfy the scope of the claims, the specific surface area thereof satisfies the scope of the claims, and forms
  • the three-dimensional tertiary channel of the claims and the tertiary channel content are in accordance with the preferred ranges recited in the claims, wherein Examples 25-26 are in a more preferred range and therefore all exhibit superior performance.
  • Comparative Example 19-20 forms a three-dimensional tertiary channel, since the ratio of organic templating agent to water does not satisfy the scope of the claims, Comparative Example 19 has too little organic templating agent to form a sufficient pore structure, while Comparative Example 20 Excessive organic templating agent, and calcination time not meeting the time range stated in the claims, results in a specific surface area of Comparative Examples 19-20 which is lower than the scope of the claims, thereby exhibiting a low conversion rate and a selection of lower olefins. The properties are also much lower than the catalyst of the present invention.
  • the preparation process of the catalyst is basically the same as that of the embodiment 5, except that the metal element in the multi-metal composite is replaced, and the copper nitrate hexahydrate is replaced with sodium hydrogencarbonate when the metal precursor solution is disposed to ensure the atom replacement of the metal.
  • the atom of the replaced metal is (1:10), and the cobalt nitrate hexahydrate is replaced with ferric ammonium citrate to ensure that the atom of the replacement metal and the atom of the replaced metal are (1:2).
  • the preparation process of the catalyst is basically the same as that of the embodiment 27, except that the metal element in the multi-metal composite is replaced, and the sodium hydrogencarbonate is replaced with the basic magnesium carbonate when the metal precursor solution is disposed, and the atom of the replacement metal is ensured.
  • the atom of the replaced metal is (1:1).
  • the catalyst preparation process was basically the same as that of Example 27 except that the metal element in the multi-metal composite was replaced, and sodium hydrogencarbonate was replaced with potassium nitrate when the metal precursor solution was disposed, and the atom of the replacement metal was replaced.
  • the atom of the metal is (1:1).
  • the catalyst preparation process is basically the same as that of Example 27 except that the metal element in the multi-metal composite is replaced, and the sodium hydrogencarbonate is replaced with lanthanum nitrate when the metal precursor solution is disposed to ensure that the atom of the replacement metal is replaced.
  • the atom of the metal is (1:1).
  • the catalyst preparation process is basically the same as that of Example 27 except that the metal element in the multi-metal composite is replaced, and the sodium hydrogencarbonate is replaced with lanthanum nitrate when the metal precursor solution is disposed to ensure that the atom of the replacement metal is replaced.
  • the atom of the metal is (1:1).
  • the catalyst preparation process is basically the same as that of the embodiment 5 except that the metal element in the multi-metal composite is replaced, and the copper nitrate hexahydrate is replaced with 25 wt.% manganese nitrate when the metal precursor solution is disposed to ensure replacement of the metal.
  • the atom with the replaced metal is (1:1)
  • the cobalt nitrate hexahydrate is replaced with ferric ammonium citrate to ensure that the atom of the replacement metal and the atom of the replaced metal are (1:2)
  • the ⁇ -Al 2 O 3 is made of nitric acid.
  • Gallium replacement ensures that the atoms of the replacement metal and the atoms of the replaced metal are (1:1).
  • the preparation process of the catalyst is basically the same as that of the embodiment 32, except that the metal element in the multi-metal composite is replaced, and the gallium nitrate is replaced with zirconium nitrate when the metal precursor solution is disposed to ensure the replacement of the metal atom and the replaced metal.
  • the atom is (1:1).
  • the preparation process of the catalyst is basically the same as that of the embodiment 32, except that the metal element in the multi-metal composite is replaced, and the gallium nitrate is replaced with indium nitrate when the metal precursor solution is disposed to ensure the replacement of the metal atom and the replaced metal.
  • the atom is (1:1).
  • the catalyst preparation process was basically the same as that of Examples 27-31 except that the metal elements in the multi-metal composite were replaced, and the zinc nitrate was replaced with 25 wt.% manganese nitrate when the metal precursor solution was disposed to ensure replacement of the metal.
  • the atom and the atom of the replaced metal are (1:1).
  • a mixture obtained by mechanically mixing a commercial Na-ZSM-5 molecular sieve with a composite oxide of Co 0.1 Cr 3 Zn 2 prepared by a coprecipitation method as a catalyst under the same conditions, the selectivity of lower alkanes and alkenes does not exceed 20%, produced a large amount of methane and the stability of the catalyst was extremely poor, and it was inactivated in 15 hours.
  • the molecular sieve contains only a microporous structure and does not have a mesoporous structure, and the carbon formed by the reaction easily blocks the micropores, thereby causing deactivation.
  • the FeN nanoparticles are supported in the lumen, which can limit the aggregation and growth of the nanoparticles and avoid deactivation.
  • K and Mn are promoted, K 0.4 Mn 1.0 FeN@CNTs can be obtained, and low-carbon olefins can be selectively formed. .
  • the selectivity of the C 2 -C 4 in the total hydrocarbon product can be as high as 60 to 95%, and the selectivity of the lower olefin in the total hydrocarbon product is as high as 50 to 85%. Since the surface of the catalyst metal complex does not activate hydrogen molecules, a large amount of methane is prevented from being generated, and the selectivity of methane selectivity and C 5+ long carbon chain hydrocarbons can be extremely low, and both are less than 10%.
  • the multi-stage pore structure of the inorganic solid acid avoids catalyst deactivation, and the conversion of CO for 100 hours in a continuous reaction is stable, and the product selectivity is stable.
  • the selectivity of methane selectivity and C 5+ long carbon chain hydrocarbons is extremely low, a total of 5 to 10%.
  • the intermediate species formed on the surface are weakly adsorbed, easily desorbed from the surface and diffused into the pores of the inorganic solid acid, and further converted into low-carbon hydrocarbons by the acid sites.
  • the inorganic solid acid of the present invention has a multi-stage pore structure, thereby avoiding catalyst deactivation, stable conversion of CO for 100 hours in continuous reaction, and stable product selectivity.
  • the conventional microporous MTO molecular sieve catalyst does not have a multi-stage pore structure, and is easily cleaved by the intermediate species formed by the reaction, resulting in rapid deactivation of the catalyst, and is not conducive to direct mixing of the mass transfer to obtain only alkanes, and almost no olefins are produced.
  • the Fe-based catalyst still follows the Fischer-Tropsch reaction mechanism, that is, CO dissociates and adsorbs on the surface of the catalyst to form surface carbon and surface oxygen, and surface oxygen reacts with the adsorbed hydrogen to form water, and the surface carbon and surface Hydrogen reacts to form CHx.
  • CHx is strongly adsorbed on the surface, and a plurality of surface CHx are polymerized to cause chain growth.
  • the hydrocarbons of different carbon chain lengths are determined by the surface properties of the catalyst and desorbed into the gas phase.
  • the method has the characteristics of simple process and low equipment investment, and has important application prospects.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Health & Medical Sciences (AREA)
  • Plasma & Fusion (AREA)
  • Toxicology (AREA)
  • Optics & Photonics (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

本发明公开了一种合成气一步法直接制低碳烯烃的催化剂及其方法，具体地说，涉及一种连续流动条件下，将合成气一步法直接转化为低碳烯烃的方法及其催化剂，所提供的催化剂为多组分金属复合物和多级孔结构的无机固体酸构成的复合材料，无机固体酸具有微孔、介孔和大孔的多级孔结构，金属复合物分散在无机固体酸表面或孔道中，可以催化合成气转化生成含2个到4个碳原子的C 2-C 4低碳烃类产物，CO单程转化率为10～60％，低碳烃在所有碳氢化合物产品中的选择性可高达60～95％，其中低碳烯烃(C 2 ＝-C 4 ＝)的选择性为50～85％。

Description

一种催化剂及由合成气一步法直接制备低碳烯烃的方法 技术领域
本发明属于制备低碳烯烃领域，具体涉及一种由合成气一步法制备低碳烯烃的方法及其催化剂。
背景技术
低碳烯烃包括乙烯、丙烯、丁烯，是合成塑料、纤维和各类化工材料的重要原料，随着国民经济的增长，其消费需求也越来越快。目前，低碳烯烃主要由石脑油裂解的石油化工路线生产获得。随着全球石油资源日渐消耗和居高不下的原油价格，尤其对石油资源匮乏的我国而言，每年超过近60％的石油消耗量依赖进口，我国低碳烯烃生产的原料70％为原油炼制得到的石脑油和轻烃，寻求一种可以替代的工艺路线，开发利用由煤、生物质等非油基碳资源制备低碳烯烃的方法，具有重要的社会意义和战略意义。
我国煤炭资源丰富，以煤炭为原料，经过气化得到合成气(即CO和H2的混合气)，再将合成气转化制甲醇，甲醇制烯烃(MTO)的工艺成熟，已经步入工业化。催化剂为改性的分子筛SAPO-34或ZSM-5，甲醇转化率接近100％，乙烯和丙烯选择性85-90％，仅有少量的C5+以上长碳链碳氢化合物生成。2010年8月，世界首套基于大连化物所具有自主知识产权的甲醇制烯烃(DMTO)技术的工业装置成功实现商业运转，标志着我国煤制烯烃新兴产业取得了里程碑式的进展。2015年4月，同样采用大连化物所核心技术的浙江兴兴新能源60万吨/年MTO装置投入商业运营，是我国第八套大型煤基甲醇制烯烃工业装置。
与经甲醇制烯烃的间接途径相比，从合成气一步法直接制备烯烃的路线则具有工艺简单，设备投资少的特点，国内外科研院所以及企业投入了大量了资源，开展合成气一步法制低碳烯烃工艺路线的研究。中国石化上海石油化工研究院对合成气由费托路线直接制取低碳烯烃技术的经济性进行了评估[杨学萍，董丽，化工进展31(2012)1726-1731]。当油价为110美元/桶，而煤价不高于520元/吨，烯烃在总产品中组成为30％时，煤基合成气直接制低碳烯烃的销售成本就比较有优势。若能进一步提高低碳烯烃在总产品中在含量提高至40％以上，其经济性优势将更加明显。
由合成气直接转化制低碳烯烃，可以通过传统费托反应路径获得。该反应路径中，通常认为是由CO在催化剂表面解离吸附，经历加氢生成表面吸附的CHx中间物种，然后单个碳物种逐个经表面催化插入经历聚合反应实现碳链增长，生成不同碳数的碳氢化合物。经典的产物分布遵循Anderson-Schultz-Flory(ASF)分布方程，其数学表达式为：ln(Wn/n)＝nlnP+ln[(1-P)2/P],式中，Wn为碳数n的质量分数，P为链增长几率，(1-P)为碳链终结几率，聚合度D＝1/(1-P)，一旦P确定，整个产物分布随之确定，不同碳数的碳氢化合物分布宽，可预测的C2-C4烃类选择性最高不超过58％，汽油馏分C5-C11最高选择性为45％，同时生成大量甲烷和高碳烷烃。为此，如何选择性地生成低碳烯烃一直是该领域难以克服的挑战。国内外的研究人员做了很多努力，通过修饰催化剂结构和组成，来调变其中关键步骤的相对反应速率，如甲烷化、加氢、低碳烯烃的二次反应、碳链增长等。
其中Fe基催化剂具有价廉易得、活性高和低碳烯烃选择性高等优点，是最具潜力的合成低碳烯烃催化剂。研究人员通过添加不同组成的添加剂，如碱金属K、Na和过渡金属Mn、Cu等，可以有效改善低碳烯烃的选择性。德国鲁尔化学公司开发了多组分助剂促进的Fe-Zn-Mn-K催化剂，用于低碳烯烃的合成[12]。北京化工大学张敬畅等报道 以草酸铁为前驱体制备的Fe-Mn-K/AC催化剂在空速600h-1，15bar和320℃下，CO的转化率高达97％，C2 ＝-C4 ＝在碳氢化合物中的选择性为68％[张敬畅，卫国宾，曹维良，催化学报24(2003)259-264]，超过了由ASF分布模型预测的C2-C4烃的选择性。催化剂的载体通过与Fe物种的相互作用，也对产物的选择性起重要的修饰作用。荷兰de Jong课题组最近报道以碳纳米纤维(CNF)和α-Al2O3为载体，以柠檬酸铁胺为前驱体制备的12wt％Fe催化剂，在低压(1bar)，350℃，H2/CO＝1条件下，反应15小时，CO转化率为0.5-1.0％，低碳烯烃在碳氢化合物中的选择性为60％[H.M.T.Galvis,J.H.Bitter,C.B.Hhare,M.Ruitenbeek,A.L.Dugulan,K.P.de Jong,Science 335(2012)835-838]。同样的催化剂在340℃，H2/CO＝1,20bar，空速1500h-1下，获得了70-88％的转化率，FTY分别为2.98×10-5mol CO/gFe·s和1.35×10-5mol CO/gFe·s，CO2的选择性为42-46％，其中低碳烯烃在碳氢化合物中的选择性为52-53％。随后他们发现，催化剂中的微量0.03％S，0.2％左右的Na，对反应活性和低碳烯烃的选择性具有明显的促进作用[H.M.T.Galvis,A.C.J.Koeken,J.H.Bitter,T.Davidian,M.Ruitenbeek,A.I.Dugulan,K.P.de Jong,J.Catal.303(2013)22-30]。中国科学院大连化物所对活性炭载体作了系统深入的研究，发现活性炭负载的铁催化剂上产物偏离ASF分布[沈俭一，林励吾，章素，梁东白，燃料化学学报19(1991)289-297；马文平，丁云杰，罗洪原等，催化学报22(2001)279-282]。此外，催化剂的制备方法和工艺，如焙烧过程、还原条件等，可以直接影响活性组分的分散和尺寸，从而调变反应的活性和产物的选择性。北京化工大学采用超临界流体组合技术(即化学沉淀、类凝胶、超临界干燥的方法)使活性组分Fe和助剂高度分散，制备了纳米级Fe基催化剂，CO的转化率大于96％，低碳烯烃在碳氢化合物中的选择性大于54％[北京化工大学，一种用于合成气制低碳烯烃的纳米催化剂及制备方法：中国，101396662[P].2009-04-01]。
有研究人员设法将费托反应与其它工艺进行组合，如裂解反应[J.L.Park,Y.J.Lee,K.W.Jun,J.W.Bae,N.Viswanadham,Y.H.Kim,J.Ind.Eng.Chem.15(2009)847-853]，通过双床层反应器，首先在第一个反应器Fe-Cu-Al催化剂上300℃、10atm、GHSV＝3600h-1下进行费托反应，再经过第二个反应器500℃下ZSM-5裂解催化剂床层，将大量的C5+产物裂解为低碳烯烃，由此得到的碳氢化合物产物中低碳烃的选择性为52％，低碳烯烃在总产品中的选择性为28％。
此外，由于合成气直接制甲醇和甲醇制烯烃的过程相对成熟，人们对这两个过程的耦合也做了大量的尝试。Xu等将CuO-ZnO-Al2O3与ZSM-5混合，得到的催化剂，在合成气转化反应中得到的产物主要为二甲醚[M.Xu,J.H.Lunsford,D.W.Goodman,A.Bhattacharyya,Appl.Catal.A.General 149(1997)289；D.Mao,W.Yang,J.Xia,B.Zhang,Q.Song,Q.Chen,J.Catal.230(2005)140]。Erena等将CuO/ZnO/Al2O3等多组分金属复合物与ZSM-5分子筛混合，催化合成气转化，得到的产物主要为汽油[J.Erena,J.M.Arandes,J.Bilbao,A.G.Gayubo,H.I.De Lasa,Chemical Engineering Science 2000,55,1845；J.Erena,J.M.Arandes,R.Garona,A.G.Gayubo,J.Bilbao,Journal of Chemical Technology and Biotechnology 2003,78,161]。
本发明提供了一种合成气直接转化制低碳烯烃的方法及其催化剂，得到的碳氢化合物中低碳烃，即含有2个到4个碳原子的烃类产物的选择性高达60～95％，其中低碳烯烃包括乙烯、丙烯和丁烯的选择性占50～85％。
发明内容
针对上述问题，本发明提供了一种由合成气一步法直接转化制低碳烯烃的方法及其催化剂。该方法通过一种复合催化剂材料，原料分子CO在具有缺陷位的金属复合物表 面活化，吸附的另外的CO与解离生成的氧原子反应生成CO2，由于另一个原料分子氢不能与解离的氧原子生成水，避免了大量高值的氢的消耗，这样该反应原料的氢碳比就可以非常小，理论上可以为H/C＝0.5，在这种情况下，该工艺可以直接利用煤气化炉出口的混合气，可以减除高能耗的水煤气变换工段；另一方面，在复合物表面生成的CHx中间体不能在复合物表面停留，会以自由基的形式脱附到气相中，并进入多孔材料的孔道中，进行限域的链增长，选择生成目标烃类分子，实现了一步法直接催化转化合成气，高选择性地生成低碳烯烃，这样过程不仅突破了传统费托反应路径中产物ASF分布的限制，高选择性地获得低碳烯烃，而且摒弃了额外的甲醇合成过程，以及水煤气变换过程。低碳烯烃在碳氢化合物中的选择性高达50～85％，一氧化碳的单程转化率为10～50％。该方法具有工艺简单，设备投资少的特点，可以预见，该方法可以显著降低低碳烯烃的生产成本，具有重要的应用价值。
本发明的技术方案为：
所述催化剂为多组分金属复合物和多级孔结构的无机固体酸构成的复合材料；无机固体酸具有微孔、介孔和大孔的多级孔结构；金属复合物分散在无机固体酸表面或孔道中；
按催化剂的总质量为100％计，所述多组分金属复合物在整个催化剂中的含量为10wt.％～75wt.％，优选25wt.％-75wt.％；
所述多级孔结构的无机固体酸是由无机固体酸二次粒子组成，无机固体酸二次粒子大小为100nm-500μm，优选为150nm-100μm；
所述无机固体酸二次粒子是由大小为5-200nm(优选20-120nm)的无机固体酸晶粒堆积形成的；
所述无机固体酸二次粒子具有三维三级孔道结构，包括一级孔，二级孔，三级孔三种孔道；
所述一级孔是孔道直径小于2nm范围的微孔孔道，微孔位于无机固体酸晶粒内部；
所述二级孔是孔道直径2nm-50nm的介孔孔道，优选为2-15nm，二级孔是由无机固体酸晶粒堆积而成，位于无机固体酸二次粒子内部及三级孔的孔壁上；
所述三级孔是孔道直径分布大于50nm的大孔孔道，是无机固体酸二次粒子堆积而成；
所述三种孔道之间相互连接贯通，构成三维三级孔道结构，二级孔可位于相邻三级孔孔壁，一级孔可位于相邻的二级孔和/或三级孔孔壁；
所述的多级孔结构的无机固体酸由N2物理吸附测定的BET比表面积为100～1200m2/g，孔容为0.25～0.80ml/g；按照比表面积计算，微孔占10-65％，介孔占20-75％，大孔占15-70％；优选的微孔的比表面积占10-60％，介孔比表面积占20-70％，大孔占20-70％；更优选为微孔的比表面积占10-50％，介孔比表面积占总比表面积的30-70％，大孔占20-60％。
所述的多组分金属复合物中的金属为两种或三种以上的金属元素，优选为两种至五种金属元素；所述金属复合物包括金属氧化物以及金属、金属碳化物、金属氮化物、和金属无机酸盐中的一种或二种以上；
所述金属元素包括必要金属元素以及其它元素，其中必要金属元素为Zn或Co或Cr或Mn；
若所述必要金属元素为Zn，则其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Co、Cu、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Cr、Mn、Co、Cu、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Cr、Mn、Co、Cu、Pd、Ce中的一种或二种以上；
若所述必要金属元素为Co时，其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Cr、Mn、Cu、Zn、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Cr、Mn、Cu、Zn、Pd、Ce中的一种或二种以上；
若所述必要金属元素为Cr，则其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Mn、Fe、Co、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Mn、Co、Cu、Zn、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Mn、Co、Cu、Zn、Pd、Ce中的一种或二种以上；
若所述必要金属元素为Mn，则其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、Cr、Fe、Co、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Cr、Co、Cu、Zn、In、La、Mo、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Cr、Co、Cu、Zn、Pd、Ce中的一种或二种以上；
所述的多组分金属复合物中，金属氧化物的含量为5～90％，金属和金属碳化物和金属氮化物中的一种或两种以上的总质量含量可以是小于或者等于10％，，金属无机酸盐的含量为10～95％；优选金属氧化物的含量为30-90％，金属和金属碳化物和金属氮化物中的一种或两种以上的总质量含量小于5％，金属无机酸盐的含量为10-70％；
所述的多组分金属复合物中必要元素Zn或Co或Cr或Mn与其他元素的总摩尔比为(0.1～5.0)：1，优选摩尔比为0.2～3.5；
所述无机酸盐是由阳离子与阴离子组成，其中Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Co、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、Sn、Cs、Ce中的一种或二种以上可以以阳离子形式存在，而Al、Si、V、Cr、Mn、Fe、Co、Zn、Mo、Ti、Zr、Ce、Ga、In、Ge也可以以ZnO2 2-、Al2O4 2-、SiO3 2-、SiO4 4-、TiO3 2-、TiO3 3-、VO3 -、VO3 2-、CrO4 2-、Cr2O4 2-、Mn2O4 2-、Fe2O4 2-、Co2O4 2-、Ni2O4 2-、Fe(CN)6 3-、Fe(CN)6 4-、MoO4 2-、TiO3 2-、ZrO3 2-、CeO3 2-、Ga2O4 2-、In2O4 2-、GeO3 2-、GeO4 4-、SrO3 4-中的一种或二种以上阴离子形式存在，阳离子与阴离子组成无机酸盐，无机酸盐组成如表1所列；且构成阳离子和构成阴离子的金属元素不同。
所述金属复合物是由权利要求2中所述金属氧化物以及金属、金属碳化物、金属氮化物、金属无机酸盐中一种或两种以上的晶粒相互均匀分散形成，其晶粒大小为0.5-20nm，优选1-10nm；同时这些晶粒进一步堆积形成二次粒子，二次粒子大小为10nm-200μm，二次粒子中晶粒堆积形成的孔道直径为2-20nm，优选为5-15nm。
所述的无机固体酸由H、O为必要元素，以及Al、Si、P、Zr、Ti、Ge中的一种或两种以上元素组成，形成由硅氧氢元素组成的无机固体酸、由硅铝氧氢元素组成的无机固体酸、由硅铝磷氧氢元素组成的无机固体酸、由钛硅氧氢元素组成的无机固体酸、由锆硅氧氢元素组成的无机固体酸、由锗硅氧氢元素组成的无机固体酸、由锗铝磷氧氢元素组成的无机固体酸中的一种或二种以上。
所述的多级孔结构的无机固体酸具有酸性特征；
所述的酸性位分布于权利要求1所述的三维三级孔道；
按照NH3-TPD定义酸性强弱，所述固体无机酸包含弱酸、中强酸、强酸三种酸性；
该NH3-TPD是根据NH3的脱附峰位置，所述脱附峰的位置是指在标准测试条件下，在样品质量w与载气流速f比值(w/f)＝100g·h/L，10℃/min升温速度的测试条件下，TCD记录脱附NH3的热导信号，绘制脱附曲线，根据曲线峰位置顶点将所述无机固体分为三种酸性强度；
所述弱酸是NH3脱附温度小于275℃的酸性位；
所述中强酸是NH3脱附温度在275-500℃的酸性位；
所述强酸是NH3脱附温度大于500℃的酸性位；
所述无机固体酸中，中强酸位点的量是0.06-10mol/kg；优选1-10mol/kg；
所述的多组分金属复合物和多级孔结构的无机固体酸构成复合材料；多组分金属复合物中尺寸在0.5-10nm的粒子可以位于多级孔结构的无机固体酸的微孔、介孔或者大孔孔道内以及无机固体酸外表面，多组分金属复合物中尺寸在10-200nm的二次粒子可以位于多级孔结构的无机固体酸的大孔和介孔的孔道内或者无机固体酸外表面，尺寸大于200nm的金属复合物二次粒子分散在多级孔结构的无机固体酸外表面，多组分金属复合物的外表面与无机固体酸的大孔和介孔的内表面及无机固体酸二次粒子的外表面堆积形成活性孔；所述活性孔连接金属复合物介孔与多级孔结构的无机固体酸中的三维三级孔道，使得所有孔道连通复合。
所述的多级孔结构的无机固体酸制备方法包括软模板水热法、硬模板水热法或结晶控制水热法；在软模板水热法、硬模板水热法或结晶控制水热法的老化操作中，使用恒温搅拌老化处理有利于形成多级孔结构的无机固体酸；
所述结晶控制水热法，快速老化，并在晶化过程中控制搅拌速率和温度，避免分子筛晶粒过度长大，促进小晶粒的形成，使更多的小晶粒之间产生晶间介孔，获得多级孔结构的无机固体酸，同时通过调变老化及晶化条件可以同时调变权利要求5所述的酸性强弱及中强酸的量；具体步骤包括：均匀溶胶分散液的制备、老化、晶化、洗涤、干燥和焙烧；所述的均匀溶胶分散液的制备是将无机固体酸所含有元素的前驱体按所需比例，称量后投入含有水的容器中，在室温下进行搅拌分散，同时加入有机微孔模板剂制得液相分散体系；所述老化方法是将配制好的液相分散体系在温度控制在20-60℃，时间10min-24h，搅拌速率50-1000rpm；晶化过程中搅拌速率50-500rpm，温度120-250℃，时间12h-10day；洗涤方法可以是过滤洗涤或离心洗涤，过滤洗涤应保证洗涤结束时滤液pH是6.5-7.5，离心洗涤应保证洗涤结束时上清液是6.5-7.5；所述干燥过程，温度在100-150℃，时间大于12h；所述焙烧过程，温度在500-650℃，时间1-8h；
所述软模板水热法，是利用有机介孔模板剂，使用水热法合成多级孔结构的无机固体酸，具体步骤涉及均匀溶胶分散液的制备，老化，晶化，洗涤，干燥和焙烧；所述的均匀溶胶分散液的制备是将无机固体酸所含有元素的前驱体按所需质量比，称量后投入含有水的容器中，在室温下进行搅拌分散，同时加入有机微孔模板剂及有机介孔模板剂(其质量比为0.3～0.8)，制得液相分散体系，老化过程中温度控制在20-60℃，时间10min-24h，搅拌速率50-1000rpm；晶化过程中搅拌速率50-500rpm，温度120-250℃，时间12h-10day；洗涤方法可以是过滤洗涤或离心洗涤，过滤洗涤应保证洗涤结束时滤液pH是6.5-7.5，离心洗涤应保证洗涤结束时上清液是6.5-7.5；所述干燥过程，温度在100-150℃，时间大于12h；所述焙烧过程，温度在500-650℃，时间1-8h；
所述硬模版水热法，是可以在650℃下被氧化的纳米碳材料、SBA系列、M41S系列、HMS系列、MSU系列、KIT系列、FDU系列、AMS系列、HOM系列、MCM-41介孔分子筛中的一种或两种以上作为硬模板，使用水热法合成多级孔结构的无机固体酸，具体步骤涉及均匀溶胶分散液的制备，老化，晶化，洗涤，干燥和焙烧；所述的均匀溶胶分散液的制备是将无机固体酸所含有元素的前驱体按所需质量比，称量后投入含有水的容器中进行搅拌分散，同时加入有机微孔模板剂及硬模板材料(其质量比例为0.3～0.8)制得液相分散体系，抑制晶粒长大，促进小晶粒形成介孔；温度控制在20-60℃，时间10min-24h，搅拌速率50-1000rpm；晶化过程中搅拌速率50-500rpm，温度120-250℃，时间12h-10day，洗涤方法可以是过滤洗涤或离心洗涤，过滤洗涤应保证洗涤结束时滤液pH是6.5-7.5，离心洗涤应保证洗涤结束时上清液是6.5-7.5；所述干燥过程，温度在 100-150℃，时间大于12h；所述焙烧过程，温度在500-700℃，时间1-8h；
所述均匀溶胶分散液中前驱体是水玻璃、硅溶胶、超微SiO2、白炭黑、硅酸钠、TMOS、硅酸酯、四氯化硅、高岭土、硝酸铝、硫酸铝、铝酸钠、薄水铝石、拟薄水铝石、三水铝石、三水异丙醇铝、三氯化铝、氢氧化铝、烷氧基铝、超微粉末铝、氧化铝、磷酸、磷酸铝、磷酸钠、氧化锆、硝酸锆、磷酸锆、硅酸锆、四氯化钛、钛酸丁酯、氧化钛、氧化锗、硝酸锗、氯化锗、三氯甲基锗、四乙基锗中的一种或两种以上；
所述有机微孔模板剂是TMA、TPA、TEA、TEAOH、DDO、TBA、TQA、乙二胺、吡咯烷、胆碱、PDN、RDN、PDA、季戊四醇、羟酸、丙基硫醛、三丙胺、DABCO、二正丙胺、叔丁胺、异丙胺、奎宁环、新戊胺、三乙醇胺、二环己胺、N,N-二甲基苄胺、N,N-二甲基醇胺、N,N-二乙基乙醇胺、2-甲基吡啶、哌啶、吗啡中的一种或两种以上；
所述有机介孔模板剂是CTBA、CTBABr、十二烷基磷酸酯、长链伯胺、聚氧乙烯、聚氧丙烯、聚氧乙烯嵌段醚共聚物、P123、明胶与戊二醛交联物、TPHAC中的一种或两种以上；
所述溶胶前驱体和有机模板剂(包括有机微孔模板剂和有机介孔模板剂)以及水的质量比为，溶胶前驱体：有机模板剂：水＝(20-65)：(15-50)：100。
所述催化剂中多组分金属复合物和多级孔结构的无机固体酸的复合方式包括包覆生长法，超声辅助的化学复合法，或物理复合法；
所述的包覆生长法，是在多组分金属复合物上，通过权利要求6所述的方法，在多组分金属复合物表面生长出一层覆盖率至少80％以上或者完全覆盖的多级孔结构的无机固体酸，即先制备均匀溶胶分散液，再将多组分金属复合物分散于均匀溶胶分散液中，再经过老化、晶化、洗涤，干燥和焙烧得到包覆有多级孔结构的无机固体酸的多组分金属复合物；多组分金属复合物中，由Mg、Al、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Co、Cu、Zn、Zr、Mo、Pd、Ag、Cd、In、Sn、La、Ce元素组成的金属氧化物和无机酸盐由共沉淀法、浸渍法、或超声离子交换法制备；由Li、Na、K、Ga、Ge、Cs元素组成的金属氧化物和无机酸盐由浸渍法、或超声离子交换法制备；Al、Fe、Co、Cu、Zn、Mo、Pd元素还可采用化学气相沉积法或者浸渍法制备；
所述的超声辅助的化学复合法，是在多级孔结构的无机固体酸上通过超声共沉淀法，化学气相沉积法或超声离子交换法引入多组分金属复合物复合得到；
所述的物理复合法，是通过球磨，机械混匀法，摇床，振荡混合的机械化学法对多级孔结构的无机固体酸和多组分金属复合物进行复合。
所述的超声共沉淀法，指将多组分金属复合物所需两种或三种以上的金属前驱体溶解于溶剂中，得到两种或三种以上的金属阳离子溶液，然后将多级孔结构的无机固体酸在超声搅拌条件下加入到上述溶液中，超声方法可以是bath超声或Tip超声，超声功率为1-20W/(ml样品)，频率40KHz-80MHz，沉淀温度2℃-80℃，时间2min-2h，搅拌速率50-1000rpm，混合均匀之后，按所需质量比加入沉淀剂，得到均匀的沉淀物，再经干燥、焙烧，干燥温度是80-150℃，时间大于12h，焙烧温度是300-650℃，时间1-3h；
所述超声共沉淀法中，金属前驱体选自硝酸盐、甲酸盐、醋酸盐、卤化物、羰基化合物、C1～C5有机酸盐中的一种或两种以上；沉淀剂选自碳酸铵、碳酸氢铵、碳酸锂、碳酸氢锂、碳酸钠、碳酸氢钠、碳酸钾、碳酸氢钾、碳酸镁或草酸中的一种或两种以上，优选为碳酸铵、碳酸氢铵、碳酸氢钠、碳酸氢钾，最佳为碳酸铵、碳酸氢铵、碳酸氢钠；沉淀温度控制在2～80℃的范围内，干燥温度为80～150℃，时间大于12h，焙烧温度为300～650℃，时间1-3h，焙烧气氛可以是流动的空气或者静置空气；
所述超声离子交换法是指将多组分金属复合物所需两种或三种以上的金属前驱体溶解于溶剂中，得到两种或三种以上的金属阳离子溶液，然后将多级孔结构的无机固体 酸在超声搅拌条件下加入到上述溶液中，超声方法可以是bath超声或Tip超声，超声功率为1-20W/(ml样品)，频率40KHz-80MHz，沉淀温度2℃-60℃，时间1h-12h，搅拌速率50-500rpm，再经过洗涤、干燥、焙烧，洗涤方法可以是过滤洗涤或离心洗涤，使洗涤后pH在6.5-7.5，干燥温度是80-150℃，时间大于12h，焙烧温度是300-650℃，时间1-3h；
所述物理复合中的球磨法，温度为25～100℃，载气为：a)氮气和/或惰性气体，b)氢气与氮气和/或惰性气体的混合气，其中氢气于混合气中的体积为5～50％，c)CO与氮气和/或惰性气体的混合气，其中CO于混合气中的体积为5～20％，或d)O2与氮气和/或惰性气体的混合气，其中O2于混合气中的体积为5-20％，所述惰性气体为氦气、氩气、氖气中的一种或两种以上；
所述物理复合中的机械混匀法，是指使用包括3D旋转混匀仪、行星式混匀仪、或涡轮混匀仪等混匀装置，将多组分金属复合物和多级孔结构的无机固体酸加入容器中，利用这些物料及容器的高速运动产生的挤压力、撞击力、裁剪力、摩擦力等中的一种或两种以上作用实现分离、破碎、混匀等目的，通过调变温度与载气气氛实现机械能、热能与化学能的转换，进一步增强不同组分间的相互作用；反应过程中，设置温度20-100℃，载气气氛为：a)氮气和/或惰性气体，b)氢气与氮气和/或惰性气体的混合气，其中氢气于混合气中的体积为5～50％，c)CO与氮气和/或惰性气体的混合气，其中CO于混合气中的体积为5～20％，d)O2与氮气和/或惰性气体的混合气，其中O2于混合气中的体积为5-20％，所述惰性气体为氦气、氩气、氖气中的一种或两种以上。
使用任一所述催化剂进行催化反应，在所需反应温度、反应压力条件下，反应原料气体H2/CO体积比＝0.5/1～4/1，制备C2-C4低碳烯烃，即含有两个碳原子至四个碳原子数的烯烃，包括乙烯、丙烯和丁烯中的一种或者一种以上。
所述催化反应，进行该反应前，包括一个催化剂预处理过程，预处理气氛为a)H2和CO的混合气，其中H2/CO体积比为0.5/1～4/1；
或，b)氢气与惰性气体的混合气；b)中，氢气在混合气中的体积百分比为5～100％，惰性气体为氮气、氦气、氩气或氖气中的一种或两种以上；
或，c)CO与惰性气体的混合气；c)中，CO在混合气中的体积百分比为5～100％，惰性气体为氮气、氦气、氩气或氖气中的一种或两种以上；
所述催化剂预处理的温度为250～600℃，预处理压力为0.1～3.0MPa，预处理的空速为500～5000h-1，空速优选为1000～4000h-1；
所述金属复合物经过含氢气或一氧化碳的气氛还原活化之后，表面结构中具有氧空位，即氧为配位不饱和状态，可高效地催化活化CO生成中间态物种CHx(其中x＝1,2或3)中的一种或两种以上的物种，表面氧物种与CO反应生成CO2，这些极其活泼的CHx物种与CO结合生成CHxCO，生成的中间态物种在表面为弱吸附，极易从表面脱附并扩散至无机固体酸的孔道内，被进一步催化转化反应生成低碳烃，无机固体酸的孔道大小和酸性可以调变低碳烃的选择性以及其中烯烃和烷烃的相对比例。
所述反应原料气体为混合气，混合气中含有H2、CO、以及其他气体，其他气体为惰性气体和/或非惰性气体中的一种或者两种；
所述惰性气体为氮气、氦气、氩气、氖气中的一种或两种以上，在反应原料气体中的体积含量小于10％；
所述非惰性气体为二氧化碳、气化的水、甲醇、乙醇中的一种或者两种，在反应原料气体中的体积含量小于50％。
H2与CO的体积比H2/CO为0.5/1～4/1。
所述反应采用的装置为流化床、移动床或固定床；
所述反应温度为300～500℃，反应温度优选为350～450℃，空速为500～10000h-1，空速优选为2000～7000h-1；
所述反应为连续流动反应模式或间歇反应模式；
所述连续流动反应模式中，反应压力为0.1～6.0MPa，反应压力优选为1.0～5.0MPa；
所述间歇反应模式中，反应压力为1.0～10MPa，反应压力优选为1.0～5.0MPa。
表1无机酸盐的阳离子和阴离子列表
Figure PCTCN2015092091-appb-000001
本发明涉及一种由合成气一步法直接转化制低碳烯烃的方法，低碳烯烃产物包括乙烯、丙烯和丁烯中的两种或者两种以上；低碳烯烃产物在所有碳氢化合物中含量为50～85％。
本发明的有益效果：
本发明与传统费托反应路径一步法制低碳烯烃的过程相比，具有如下特点：
1.产物不同于由链增长控制的Anderson Schultz Flory分布规律；传统费托反应产物中，可预测的C2-C4烃选择性最高为58％，而本发明提供产物中C2-C4的选择性可达60～95％；
2.低碳烯烃在总烃产物中的选择性高达50～85％；
3.产物中甲烷选择性和C5+长碳链碳氢化合物的选择性极低，两者共为5～10％；
4.催化剂不同于传统费托反应制低碳烃所用的过渡金属如Fe、Co等为主成分的催化剂，而是含多级孔结构的无机固体酸与多组分金属复合物的复合催化材料。
本发明与目前已经工业化的两段法，即先将合成气转化成甲醇或二甲醚，再将甲醇或二甲醚转化成低碳烯烃的过程相比，具有如下特点：
1.一个反应器，一个催化剂，一步法转化，可显著降低设备投资和生产成本；
2.催化剂为含多级孔结构的无机固体酸与多组分金属复合物复合而成的催化材料，产品选择性可以很好调控；
3.该催化剂稳定性好，寿命长。
4.本发明具有操作单元单一，过程重复性好，产物选择性高，催化剂寿命长(>500h)，具有广阔的工业应用前景。
本发明所用的催化剂具有如下优点：在合成气制备低碳烯烃反应中，本发明提供的催化剂为多组分金属复合物与多级孔结构的无机固体酸复合得到的复合材料。该催化剂不同于传统费托反应制低碳烃所用的过渡金属为主成分的催化剂，也不同于工业两段法 经过甲醇合成所用的催化剂，其创新之处包括结构和功能：结构方面在于催化剂同时具有微孔、介孔的多级孔结构，这种独特结构使催化剂具有显著的优势，即在反应条件下长时间运行(>500h)而不失活；功能方面在于可以直接催化合成气转化，无需配套高能耗的水煤气变换过程，无需将合成气转化成甲醇并提取甲醇的过程，也不同于传统的链增长机理，一步可以生成低碳烃产物，其选择性为60～95％，明显突破了传统费托反应中的Anderson-Schultz-Flory分布限制，且甲烷和长碳链产物(C5+)的选择性低于5～10％。
附图说明
图1实施例8中核壳结构的Cr1Zn1@SiAl的SEM图；
图2实施例8中Cu1Zn1@SiAl的XRD图；
图3实施例14中多级孔结构的硅磷铝无机固体酸的N2物理吸附曲线及其孔径分布图；
图4实施例6中合成气直接转化为产物的在线色谱分析的色谱图。
具体实施方式
下面通过实施例对本发明做进一步阐述，但是本发明的权利要求范围不受这些实施例的限制。同时，实施例只是给出了实现此目的的部分条件，但并不意味着必须满足这些条件才可以达到此目的。
催化反应实例
以连续流动固定床反应为例，但是催化剂也适用于流化床反应器。该装置配备气体质量流量计、气体脱氧脱水管和在线产物分析色谱(反应器的尾气直接与色谱的定量阀连接，进行周期实时采样分析)。上述催化剂在使用前，均压片过筛至20-40目颗粒或者40-60目，备用。
将下述实施例或对比例中所述的催化剂2.8g，置于固定床反应器中，使用Ar置换反应器中的空气，然后在纯H2气氛中310～350℃下还原1h，在Ar气氛中降至室温，再切换合成气(5％Ar；H2/CO＝2/1)，升温至反应温度，调节反应原料气的空速、压力。产物由在线色谱检测分析。改变温度、压力、空速和H2/CO比例，可以改变反应性能。
实施例1
化学复合法制备多组分金属复合物-多级孔结构的硅铝无机固体酸复合催化剂。
以CuZnAl多组分金属复合物，多级孔结构的硅铝无机固体酸为例。
按氧化物SiO:Al2O3:Na2O:R2O:H2O＝40:1:16:5:900(质量比)称取原料：硅溶胶30％(质量浓度)；硫酸铝；氢氧化钠；N,N,N-一三甲基金刚烷氢氧化铵(R)；去离子水，室温混合后，在60℃,200rpm速度搅拌24h后转移到水热釜中，155℃下晶化6天。自然冷却到室温，转移到烧杯中水浴70℃，按100ml原液：4g氯化铵的比例加入氯化铵，恒温搅拌3h，反复离心洗涤使得洗涤结束时上清液pH是7，沉淀物于120℃下烘干24h后，在650℃空气中焙烧3h得到多级孔结构的硅铝无机固体酸。
称取制备好的多级孔结构的硅铝无机固体酸5.3g，取三水合硝酸铜1.2g，六水合硝酸锌1.49g，九水合硝酸铝1.8g，溶解于100ml水溶液中，通过浸渍法将CuZnAl引入到多级孔结构的硅铝无机固体酸上，并经过室温真空干燥，500℃静态空气中焙烧1h，得到元素摩尔比为1:1:1的Cu1Zn1Al1/mesoSiAl，多组分金属复合物的负载量为20wt％。根据此方法，可以改变各金属组分及其比例，以及多组分金属复合物的负载量。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为347m2/g，微孔孔径分布在
Figure PCTCN2015092091-appb-000002
介孔比表面积为214m2/g，大孔比表面为62m2/g；介孔孔径大小分 布在2-15nm。X射线衍射(XRD)表征显示，多组分金属复合物含CuO、ZnO、Al2O3、ZnAlO2和具有CHA结构的硅铝无机固体酸，金属氧化物的晶粒大小5-15nm；无机固体酸晶粒大小为40-70nm；扫描电镜(SEM)表征表明，多级孔结构的硅铝无机固体酸二次粒子大小为10-100μm，无机固体酸晶粒大小为10-100nm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小5-15nm，二次粒子大小15-50nm；中强酸对应的NH3脱附峰温度为360℃，中强酸位点的量是2mol/kg。中强酸是按照NH3-TPD定义的，是根据NH3的脱附峰位置，所述脱附峰的位置是指在标准测试条件下，在样品质量w与载气流速f比值(w/f)＝100g·h/L，10℃/min升温速度的测试条件下，TCD记录脱附NH3的热导信号，绘制脱附曲线，根据曲线峰位置顶点将所述无机固体分为三种酸性强度：所述中强酸是NH3脱附温度在275-500℃的酸性位。
实施例2
制备过程与实施例1基本相同，不同之处制备实施例1中多级孔结构的硅铝无机固体酸的制备过程中，改变晶化温度为150℃，5天，制备出中强酸位点的量是0.8mol/kg的CHA结构的硅铝无机固体酸。
作为对比例1，制备过程与实施例1基本相同，不同之处制备实施例1中多级孔结构的硅铝无机固体酸的制备过程中，晶化温度为140℃，3天，制备出中强酸位点的量是0.01mol/kg的硅铝无机固体酸。
作为对比例2，制备过程与实施例1基本相同，不同之处制备实施例1中多级孔结构的硅铝无机固体酸的制备过程中，晶化温度为140℃，22h，制备出中强酸位点的量是0.005mol/kg的硅铝无机固体酸。
在365℃，2MPa体积空速4000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000003
对比例1，2中转化率极低，这是由于固体酸中中强酸位较少，导致多组分金属复合物上产生的中间物种不能被及时、很好地转化成为目标产物。同时甲烷选择性大大提高，超过30％，而低碳烯烃选择性也降低的很明显。相比之下，含有较多中强酸的本发明催化剂，转化率大大提高，而且目标产物烯烃的选择性也高。实施例1转化率明显高于实施例2的转化率因为该催化剂是优选范围内。可见多级孔结构的硅铝无机固体酸的酸性含量对催化性能包括转化率和选择性的调控极其重要。
实施例3
化学复合法制备多组分金属复合物-多级孔结构的硅磷铝无机固体酸复合催化剂
按氧化物SiO:Al2O3:H3PO4:R:H2O＝18:16:32:55:150(质量比)称取原料：硅溶胶30％(质量浓度)；硫酸铝；磷酸；TEA(R)；去离子水，室温混合后，在30℃下搅拌老化，500rpm速度搅拌72h后转移到水热釜中，220℃下晶化15h。水浴骤冷到室温，反复离心洗涤使得洗涤结束时上清液pH是7，沉淀物于130℃下烘干17h后，在580℃空 气中焙烧5h得到多级孔结构的硅磷铝无机固体酸。
称取所述多级孔结构的硅磷铝无机固体酸2.1g，取六水合硝酸锌1.54g、九水合硝酸铬3.8g，溶解于水溶液中配成混合液A，称取6.3g碳酸铵，溶解于100ml水中配成溶液B，50℃下将溶液B逐滴加入以7W功率tip超声，400rpm速度搅拌混合液A中，离心洗涤使得洗涤结束时上清液pH是7并经过110℃空气中干燥，500℃静态空气中焙烧2h，得到ZnCr1.8/SiPAl。然后，以此为载体，准确称取0.057g醋酸钯Pd(Ac)2溶解在丙酮中，通过浸渍引入到ZnCr1.8/SiPAl上，其中Pd与Zn的摩尔比为0.01，得到元素摩尔比为0.01:1:1.8的Pd0.01ZnCr1.8/SiPAl，多组分金属复合物的负载量为20wt％。根据此方法，可以改变各金属组分及其比例，以及多元金属复合物的负载量。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔孔径分布在
Figure PCTCN2015092091-appb-000004
介孔孔径大小分布在2-8nm，总的比表面积为416m2/g，其中介孔比表面积占总比表面积的35％，大孔比表面占总面积20％，X射线衍射(XRD)表征显示，多组分金属复合物含Cr2O3、CrO3、ZnO、Al2O3、ZnCr2O4，和CHA结构的硅铝无机固体酸，金属氧化物晶粒大小7-16nm，无机固体酸晶粒大小为50-60nm；扫描电镜(SEM)表征表明，硅铝无机固体酸二次粒子大小为100-500μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小7-16nm，二次粒子大小20-100nm；中强酸对应的NH3脱附峰温度为386℃，中强酸位点的量是6mol/kg。
实施例4
制备过程与实施例3基本相同，不同之处将硅铝无机固体酸制备时，改变搅拌时间改变为3h，晶化时间变为24h，制备出总比表面积为377m2/g，介孔比表面积占总比表面积的21％，大孔比表面积占总比表面积的20％的CHA结构硅铝无机固体酸；中强酸对应的NH3脱附峰温度为385℃，中强酸位点的量是5.8mol/kg。
作为对比例3，制备过程与实施例3基本相同，不同之处在于制备硅铝无机固体酸时，老化温度改为80℃，搅拌2天后，在240℃下晶化24h，获得总比表面积为232m2/g，介孔比表面积占总比表面积的4％，大孔比表面积占总比表面积的1％，的CHA结构硅铝无机固体酸；中强酸对应的NH3脱附峰温度为411℃，中强酸位点的量是2mol/kg。
作为对比例4，制备过程与实施例3基本相同，不同之处在于制备硅铝无机固体酸时，老化温度改为30℃，搅拌2天后，在240℃下晶化48h，获得总比表面积为287m2/g，介孔比表面积占总比表面积的10％，大孔比表面积占总比表面积的4％的CHA结构硅铝无机固体酸；中强酸对应的NH3脱附峰温度为390℃，中强酸位点的量是5mol/kg。
作为对比例5，制备过程与对比例3基本相同，不同之处在于制备硅铝无机固体酸时，按照比表面积计算，利用介孔分布在4-8nm的商品SBA-15分子筛与对比例3中硅铝无机固体酸机械混合，混合比例按照硅铝无机固体酸与SBA-15比表面积为13:7，然后进行研磨混合，得到具有介孔与微孔复合物的硅铝无机固体酸，其中微孔占总比表面积的62％，介孔比表面积占总比表面积的36％，大孔占总比表面积的2％。但直径2nm-50nm的介孔孔道不是由无机固体酸晶粒堆积而成，其中一级孔不位于相邻的二级孔和/或三级孔孔壁，而是一级孔自己孤立存在，而二级三级孔道孤立存在，不符合权利要求所述的三种孔道之间相互连接贯通，未构成三维多级孔道结构。
在400℃，2.5MPa体积空速4000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000005
Figure PCTCN2015092091-appb-000006
实施例3中低碳烯烃的选择性明显优于对比3、4中的选择性，而实施例3中的选择性比实施例4中的更优，这是由于实施例3催化剂的中硅铝无机固体酸介孔比表面积占总比表面积的35％，大孔比表面占总面积20％，相比实施例4中介孔比表面积占总比表面积的21％，大孔比表面积占总比表面积的20％，在更加优选的范围内，所以传质更优，抑制了加氢产生烷烃，选择性大幅提高。而对比例中低碳烯烃的选择性远低于本发明的催化剂，这是由于分子筛中介孔及大孔过少，没有达到权利要求所述的介孔与大孔的含量，不利于传质，同时酸强度的变化也使得产物过度加氢产生烷烃，大大降低了低碳烯烃的选择性。而对比例5中虽然介孔与大孔的含量复合权利要求所述的范围，但是其含有的三种孔道直接没有相互连接贯通，未构成权利要求所述的三维三级孔道结构，另外SBA-15本身表面及其孔道内，中强酸很少，所以对比例5中的中强酸主要分布在微孔中，而不是均匀分布在所述的三维三级孔道内不符合权利要求5所述，所以与对比例3相比没有实质性的改变，低碳烯烃的选择性仍然很低。相比之下，介孔比表面积占20-75％，大孔占20-65％构成三维多级孔道结构的催化剂上，烯烃的选择性超过60％，不仅远高于对比例3,4，也高于传统费托合成的低碳烯烃的理论选择性58％，可见无机酸的孔道结构对产物选择性的调控极其重要。
实施例5
物理复合法制备多组分金属复合物-多级孔结构的硅磷铝无机固体酸复合催化剂该方法包括通过球磨，机械混匀仪，摇床，振荡混合等机械化学方式对不同材料进行混合的方法。
多级孔结构的硅磷铝无机固体酸：以三乙胺、明胶与戊二醛的交联物作为模板。将10g异丙醇铝、5.30g浓磷酸、3.67g硅溶胶(含30％质量浓度)、1.46g三乙胺、13.2g H2O混合，于室温搅拌3h，搅拌速度400rpm，然后加入1.68g 2wt％的明胶溶液，升温到57℃，继续搅拌0.5h。将得到的混合液倒入培养皿中，于0℃冷冻12h，得到冻胶，加入适量的5wt％戊二醛进行交联反应，反应后的悬浮液于10000rpm离心，得到的固体样品置于50℃烘箱中干燥过夜后，装入聚四氟乙烯内衬中，再将此小内衬放入大号聚四氟乙烯内衬中，大号内衬中需预先加入适量三乙胺与水的混合液，然后大小内衬一起装入不锈钢自压晶化釜中，于200℃干胶法晶化36h，反复离心洗涤使得洗涤结束时上清液pH是7，沉淀物于90℃下烘6h，在110℃下烘干12h后，在550℃空气中焙烧3h，得到多级孔结构的硅磷铝无机固体酸。
按照金属元素Zn:Cu:Co:Cr:Al摩尔比为6:0.2:1:1:1的比例分别称取六水合硝酸锌17.33g，六水合硝酸铜，六水硝酸钴，九水合硝酸铬，溶于100ml去离子水中，加入γ-Al2O3，于25℃下超声搅拌，tip超声功率5W，搅拌速率300rpm，然后110℃空气中干燥，500℃焙烧，得到元素摩尔比为6:0.2:1：1:1的多组分金属复合物Zn6Cu0.2Co1Cr1Al1。取该多组分金属复合物2g，多级孔结构的硅磷铝无机固体酸5g，置于聚四氟乙烯混匀罐中，首先用氦气将其中的空气置换3次，通入2％H2(He平衡)之后闭上混匀罐，开始混匀处理，速率为450转/分钟，5分钟后结束，制得复合催化剂Zn6Cu0.2Co1Cr1Al1/SiPAl，其中多组分金属复合物占催化剂的总质量40wt％。依此方法， 可以改变多组分金属复合物的含量和多级孔结构的无机固体酸的种类。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为243m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000007
介孔比表面积为318m2/g，大孔比表面为182m2/g，介孔孔径大小分布在15-25nm。中强酸对应的NH3脱附峰温度为367℃，中强酸位点的量是1.5mol/kg。
实施例6，制备过程与实施例5基本相同，不同之处在于按催化剂的总质量为100％计，将多组分金属复合物的含量调为15wt.％。
作为对比例6，制备过程与实施例5基本相同，不同之处在于按催化剂的总质量为100％计，将多组分金属复合物的含量调为5wt.％。
作为对比例7，制备过程与实施例5基本相同，不同之处在于按催化剂的总质量为100％计，将多组分金属复合物的含量调为90wt.％。
实施例7
制备过程与实施例5基本相同，不同之处在于多级孔结构的硅磷铝无机固体酸制备中更改晶化温度为190℃，时间为33h，焙烧温度600℃，时间3h。氮气物理吸脱附表征显示该催化剂具有多级孔结构，介孔孔径大小分布在10-15nm。扫描电镜(SEM)表征表面，硅铝无机固体酸二次粒子大小为10-70μm，无机固体酸晶粒大小为60-80nm；中强酸对应的NH3脱附峰温度为385℃，中强酸位点的量是1.5mol/kg。
作为对比例8，制备过程与实施例7基本相同，不同之处在于多级孔结构的硅磷铝无机固体酸制备中更改晶化温度为160℃，时间为24h，焙烧温度550℃，时间8h，流动空气下进行焙烧。氮气物理吸脱附表征显示该催化剂具有多级孔结构，介孔孔径大小分布在2-5nm。扫描电镜(SEM)表征表面，硅铝无机固体酸二次粒子大小为5-100nm；XRD显示无机固体酸晶粒大小为1-5nm；中强酸对应的NH3脱附峰温度为349℃，中强酸位点的量是0.06mol/kg。
在370℃，2MPa体积空速6000h-1的反应条件下，反应结果如下表
Figure PCTCN2015092091-appb-000008
对比例6，7中转化率远远低于实施例中的转化率，且对比例6中的甲烷选择性高达70％，而对比例7中的碳5以上的选择性超过40％，低碳烯烃的选择性也都低于本发明催化剂的结果，这是由于对比例的多组分金属复合物在整个催化剂中的含量不符合权利要求书所述的含量范围，不利于反应过程中生成的中间物种的转化。而实施例5与实施例6比较，二者的低碳烯烃的选择性都超过了50％，且甲烷选择性都低于5％，但是实施例5的转化率更高，这是因为实施例5中多组分金属复合物在整个催化剂中的含量在 优选范围，所以，转化率更高。
实施例6，7中多级孔结构的硅磷铝无机固体酸的晶粒大小及其堆积成的二次粒子大小及介孔孔道大小都复合权利要求的范围，但相对于实施例6，实施例7的晶粒大小，二次粒子大小及介孔孔道在优选范围，所以表现出了更好的转化率及选择性，而对比例8中因为不符合权利要求的范围，表现为无机固体酸结晶程度不佳，进而不能很好的进行催化转化，所以转化率，选择性都明显要差很多。所以无机固体酸的晶粒尺寸及二次粒子尺寸以及介孔孔道的尺寸都对催化转化及产物选择性的调控至关重要。
实施例8
包覆生长法制备多组分金属复合物-多级孔结构的无机固体酸复合催化剂。
该方法涉及在制得的多元金属复合物上，通过水热等方式生长出一层或部分的多级孔结构的无机固体酸材料得到。
以CuZn金属和共沉淀法为例，方法不限于双金属，且适用于其它金属，并可以改变不同金属的相对比例，可用氨水、碳酸铵或碳酸氢铵作为沉淀剂。
称取三水合硝酸铜4.8g，六水合硝酸锌5.95g溶于100ml去离子水中。称取碳酸铵11g溶于去离子水100ml中。两组溶液同时滴加到70℃恒温超声搅拌的去离子水中共沉淀，超声功率是5W，搅拌速率500rpm。然后维持70℃老化3h，用70℃去离子水洗涤到中性。然后，在110℃下干燥12h，经过500℃下焙烧1h，制备得到CuZn复合氧化物，其中Cu/Zn摩尔比为1/1。依此方法，可得到不同摩尔比的CuZn氧化物。
取10ml硅溶胶溶液(含30wt％SiO2)，加入10ml去离子水中，称取1g上述多组分金属复合物加入其中，摇床浸润2h，分离固体液体，放入120℃烘箱干燥12h，在马弗炉中500℃下焙烧2h，使上述氧化物外面覆盖一层SiO2膜，进一步取11.37g TPAOH，9.68g乙醇，0.06g三氧化二铝，50ml H2O搅拌溶解。加入上述氧化物，搅拌，称取9.65g TEOS滴加至上述溶液中，搅拌6h。在180℃下晶化72h，过滤洗涤，60℃烘箱干燥，500℃下焙烧5h，得到具有核壳结构的Cu1Zn1@SiAl催化剂，其中氧化物占催化剂总质量为50wt％。根据此方法，可以改变各金属组分及其比例，以及多元金属复合物的负载量。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为311m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000009
介孔比表面积为203m2/g，与大孔比表面为171m2/g，介孔孔径大小分布在13-30nm。X射线衍射(XRD)表征显示，多组分金属复合物含CuO、ZnO和呈MFI结构的硅铝无机固体酸，金属氧化物晶粒大小8-20nm，无机固体酸晶粒大小为55-70nm；扫描电镜(SEM)观察硅铝无机固体酸二次粒子大小为30-60μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小8-20nm，二次粒子大小20-100nm；中强酸对应的NH3脱附峰温度为408℃，中强酸位点的量是0.7mol/kg。
实施例9
制备过程和方法与实施例8基本相同，不同之处在于多元金属复合物的制备过程中，更换前驱物为六水合硝酸锌，六水合硝酸钴，九水合硝酸铝，其中六水合硝酸锌质量是5.95g，按照元素摩尔比为Zn：Co：Al＝1:0.01:1称量前驱体溶于100ml去离子水中。称取碳酸铵14.3g溶于去离子水100ml中。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为297m2/g，微孔孔径分布在
Figure PCTCN2015092091-appb-000010
介孔比表面积为122m2/g，大孔比表面为111m2/g，介孔孔径大小分布在2-8nm。X射线衍射(XRD)表征显示，多组分金属复合物含Co3O4、Co2O3、ZnO、Al2O3、ZnCo2O4和CHA结构的硅铝无机固体酸，金属氧化物晶粒大小9-17nm，无机固体酸晶粒大小为50-60nm；扫描电镜(SEM)表征表明，硅铝无机固体酸二次粒子大小为 100-500μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小9-17nm，二次粒子大小20-100nm；中强酸对应的NH3脱附峰温度为363℃，中强酸位点的量是0.6mol/kg。
作为对比例9，制备过程与实施例8基本相同，不同之处在于合成多元金属复合物过程中，不使用超声处理，在90℃老化0.5h，且焙烧温度改为300℃，使得最终催化剂不能形成很好的晶型，导致最后获得的晶粒大小<1nm。在包覆无机固体酸的过程中控制焙烧时间为1.5h。最终催化剂的微孔比表面为148m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000011
介孔比表面积为27m2/g，大孔比表面为7m2/g，介孔孔径大小分布在20-47nm。金属氧化物晶粒大小<1nm，二次粒子大小10nm-50μm；无机固体酸晶粒大小为53-79nm；无机固体酸二次粒子大小为300-600μm；中强酸对应的NH3脱附峰温度为410℃，中强酸位点的量是0.05mol/kg。
作为对比例10，制备过程与实施例8基本相同，不同之处在于合成多元金属复合物过程中，超声处理功率0.5W，在30℃老化3天，且焙烧温度改为800℃，使得最终催化剂的晶粒大小>30nm。最终催化剂的微孔比表面为757m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000012
介孔比表面积为147m2/g，大孔比表面为150m2/g，介孔孔径大小分布在8-14nm。金属氧化物晶粒大小30nm-70nm，二次粒子大小100nm-50μm；无机固体酸晶粒大小为80-120nm；无机固体酸二次粒子大小为200-800μm；中强酸对应的NH3脱附峰温度为430℃，中强酸位点的量是4mol/kg。
实施例8、对比例9和对比例10，在370℃，2MPa体积空速7000h-1的反应条件下，反应结果如下表。
实施例9在400℃，2.5MPa体积空速4000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000013
对比例9多元金属复合物的晶粒大小都非常小，其中很多金属甚至以单原子或者少量原子形成的原子簇形式存在，粒子大小小于权利要求所述的优选范围也小于权利要求所述的晶粒大小范围，对比例9反应结果虽然转化率有所增加，但甲烷选择性大大增加超过30％，同时低碳烯烃选择性下降到不足20％。而对比例10中，多元金属复合物的晶粒大小大于权利要求所述的晶粒大小范围上限，粒子过大，比表面积降低，导致其活化转化合成气能力不足，转化率非常低，同时加氢比较严重，低碳烯烃的选择性也有所下降。所以金属复合物的晶粒大小对于调控催化性能至关重要。
实施例10
制备过程和方法与实施例5基本相同，不同之处在于多元金属复合物的制备过程为，分别称取六水合硝酸锌17.33g，六水硝酸钴0.17g，氯化钛22.1g，溶于300ml去离子水中，称取碳酸铵60.5g溶于去离子水300ml中。两组溶液同时滴加到70℃恒温超声搅拌的去离子水中共沉淀，超声功率是5W，搅拌速率500rpm。然后维持70℃老化3h，用70℃去离子水洗涤到中性。然后，在110℃下干燥12h，经过500℃下焙烧1h，制备得到ZnCo0.05Ti2复合氧化物，其中Co/Ti/Zn元素摩尔比为0.05/2/1。 依此方法，可得到不同摩尔比的ZnCoTi氧化物。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为251m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000014
介孔比表面积为213m2/g，大孔比表面为216m2/g，介孔孔径大小分布在4-13nm。X射线衍射(XRD)表征显示，多组分金属复合物含ZnO、Co3O4、TiO2、ZnCo2O4和呈CHA结构的硅铝无机固体酸，金属氧化物的晶粒大小8-20nm，无机固体酸晶粒大小为60-80nm；扫描电镜(SEM)表征表面，硅铝无机固体酸二次粒子大小为300-700μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小8-20nm，二次粒子大小30-120nm；中强酸对应的NH3脱附峰温度为377℃，中强酸位点的量是2mol/kg。
作为对比例11，制备过程与实施例10基本相同，不同之处在于称量金属前驱体时，改变多元金属复合物中金属元素的比例为Zn0.05Co3Ti2，按照此比例配置金属前驱体溶液进行合成。XRD表征显示，多组分金属复合物含有ZnO、CoO、Co、ZnCo2O4、CoTiO3，且按原子数量计，金属Co含量在所有金属原子中达到30％，超过了权利要求所述的10％。多组分金属复合物的晶粒大小8-40nm，二次粒子大小30-120nm。
在400℃，2MPa体积空速6000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000015
对比例11,在相同条件下反应产物中碳5以上产物超过50％，且甲烷也超过20％，因为其中金属态的Co含量过高，不在权利要求的范围内，使得反应趋向于常规的费托合成路径，产物受到ASF分布的限制，导致低碳烯烃选择性低，而生成了较多长碳链的碳氢化合物。
实施例11
制备过程和方法与实施例8基本相同，不同之处在于得到的多级孔结构的硅磷铝无机固体酸，按照质量比1：500至于10％硝酸铵溶液中80℃搅拌8h后，抽滤并在室温干燥后，再按照质量比1:500至于1％硝酸铜水溶液中80℃搅拌8h后，抽滤并在室温干燥后，置于110℃烘箱干燥14h后，500℃空气焙烧1h得到Cu离子交换后的多元金属复合物。
多组分金属复合物的制备过程差别在于，金属前驱体的配制过程是称取六水合硝酸锌5.95g，按照元素摩尔比为1:1称取钼酸铵，溶于100ml去离子水中。称取碳酸铵11g溶于去离子水100ml中。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为239m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000016
介孔比表面积为271m2/g，与大孔比表面为198m2/g，介孔孔径大小分布在4-13nm。X射线衍射(XRD)表征显示，多组分金属复合物含ZnO、CuO、MoO3、ZnMoO4和呈CHA结构的硅铝无机固体酸，金属氧化物的晶粒大小12-26nm，无机固体酸晶粒大小为60-90nm；扫描电镜(SEM)表征表面，硅铝无机固体酸二次粒子大小为300-700μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小12-26nm，二次粒子大小30-120nm；中强酸对应的NH3脱附峰温度为345℃，中强酸位点的量是0.5mol/kg。
实施例12
制备过程与实施例11基本一致，不同之处在于更换了多元金属复合物中的金属元 素，保证替换金属的与被替换金属的原子数量相等，在配置金属前驱体溶液时将钼酸铵替换成硝酸钒酰。
实施例13
制备过程与实施例11基本一致，不同之处在于更换了多元金属复合物中的金属元素，保证替换金属的与被替换金属的原子数量相等，在配置金属前驱体溶液时将钼酸铵替换成硝酸锰。
在360℃，0.8Mpa体积空速3000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000017
实施例11与实施例12，13差别在于更换了多元金属复合物中的金属元素组成，从Mo到V到Mn。随之低碳烯烃的选择性逐渐升高。这与权利要求所述的金属元素优选所一致。
实施例14
制备过程和方法与实施例3基本相同，不同之处在于
多级孔结构的硅磷铝无机固体酸制备过程和方法是，按照质量比SiO2：Al2O3：R：H2O＝300:15:30:100称取水玻璃，薄水铝石，乙二胺，水于250ml烧杯中50摄氏度搅拌老化1h后，在30℃下搅拌二次老化，500rpm速度搅拌72h后转移到水热釜中150℃烘箱中晶化47h，水浴骤冷到室温，反复离心洗涤使得洗涤结束时上清液pH是7，沉淀物于110℃下烘干17h后，在550℃空气中焙烧3h得到多级孔结构的硅铝无机固体酸。
多组分金属复合物其金属前驱体的配制过程是称取六水合硝酸锌5.95g，按照元素摩尔比为Zn：Pd：Zr＝1:0.01:1称取硝酸钯，五水合硝酸锆，溶于100ml去离子水中。称取碳酸铵11.3g溶于去离子水100ml中。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为239m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000018
介孔比表面积为308m2/g，与大孔比表面为161m2/g，介孔孔径大小分布在4-13nm。X射线衍射(XRD)表征显示，多组分金属复合物含ZnO、PdO、ZrO2、ZnZr2O4和呈CHA结构的硅铝无机固体酸，金属氧化物的晶粒大小12-22nm，无机固体酸晶粒大小为60-90nm；扫描电镜(SEM)表征表面，硅铝无机固体酸二次粒子大小为300-700μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小12-22nm，二次粒子大小40-120nm；中强酸对应的NH3脱附峰温度为370℃，中强酸位点的量是1.6mol/kg。
实施例15
制备过程与实施例14基本一致，不同之处在于在配置金属前驱体溶液时改变了多元金属复合物的金属前驱体的配制过程的金属元素Zn与其他元素的原子比例为5:1。
作为对比例12，制备过程与实施例14基本一致，不同之处在于在配置金属前驱体溶液时改变了多元金属复合物的金属前驱体的配制过程中金属元素Zn与其他元素的原子比例为0.05:1。
在380℃，1.5MPa体积空速8000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000019
实施例14与对比例12改变了Zn与其他元素的比例，对比例12的比例不在权利要求的比例范围，所以CO的转化率很低，而实施例15虽然比例在权利要求范围内但是不在优选范围内所以转化率也较低。
实施例16
多级孔结构的硅磷铝无机固体酸制备过程和方法与实施例3基本相同，不同之处在于将得到的多级孔的硅磷铝无机固体酸置于安瓶接入10-2pa以上的真空恒温区，对多级孔的硅磷铝无机固体酸进行加热，5℃/min升温到420℃恒温12h处理后，密封转移到Ar气氛的手套箱中，将多级孔的硅磷铝无机固体酸与氯化钼按照质量比1:0.1置于石英安瓶两侧，再次接入10-2pa真空后，对石英安瓶进行封管处理使得多级孔的硅磷铝无机固体酸与氯化钼同时被封入真空的石英安瓶内部。将内封有多级孔的硅磷铝无机固体酸与氯化钼的安瓶置于管式炉中，以10℃/min升温到400℃恒温24h后，降到室温，打破安瓶得到氧化钼载量为1％的Mo-SiAlP。
多组分金属复合物的制备过程及二者复合方式与实施例5基本一致，不同之处在于金属前驱体的配制过程是，称取六水合硝酸锌5.96g，按照元素摩尔比Zn：Al＝1:1称取九水合硝酸铝，溶于100ml去离子水中。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为533m2/g，微孔孔径分布在
Figure PCTCN2015092091-appb-000020
介孔比表面积为133m2/g，大孔比表面为118m2/g，介孔孔径大小分布在3-8nm。X射线衍射(XRD)表征显示，多组分金属复合物含MoO2、ZnO、Al2O3、ZnAl2O4和CHA结构的硅铝无机固体酸，金属氧化物晶粒大小7-12nm，无机固体酸晶粒大小为50-60nm；扫描电镜(SEM)表征表明，硅铝无机固体酸二次粒子大小为100-500μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小7-12nm，二次粒子大小20-100nm；中强酸对应的NH3脱附峰温度为344℃，中强酸位点的量是2mol/kg。
作为对比例13，制备过程与实施例16基本一致，不同之处在于更换了多元金属复合物中的金属元素，保证替换金属的与被替换金属的原子数量相等，在配置金属前驱体溶液时将硝酸锌替换成硝酸铈。
作为对比例14，制备过程与实施例16基本一致，不同之处在于更换了多元金属复合物中的金属元素，保证替换金属的与被替换金属的原子数量相等，在配置金属前驱体溶液时将硝酸锌替换成纳米二氧化钛溶胶。
在400℃，3MPa体积空速4000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000021
Figure PCTCN2015092091-appb-000022
对比例13，14不含有权利要求的必要元素，所以几乎没有催化活性。
实施例17
多级孔结构的硅磷铝无机固体酸制备过程和方法与实施例5相同，不同之处在于金属前驱体溶液配置是分别称取六水合硝酸锌1.73g，按照元素摩尔比为Zn：Ga＝1:1,称取硝酸镓1.49g，溶于100ml去离子水中，按照元素摩尔比Zn：Ti＝1:1称取并加入TiO24.65g。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为289m2/g，微孔孔径大小分布在
Figure PCTCN2015092091-appb-000023
介孔比表面积为267m2/g，大孔比表面为161m2/g，介孔孔径大小分布在5-13nm。X射线衍射(XRD)表征显示，多组分金属复合物含ZnO、Ga2O3、TiO2呈CHA结构的硅铝无机固体酸，金属氧化物的晶粒大小13-20nm，无机固体酸晶粒大小为60-80nm；扫描电镜(SEM)表征表面，硅铝无机固体酸二次粒子大小为300-700μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小13-20nm，二次粒子大小30-120nm；中强酸对应的NH3脱附峰温度为336℃，中强酸位点的量是0.47mol/kg。
实施例18
制备过程和方法与实施例3基本相同，不同之处在于制取多级孔结构的硅磷铝无机固体酸，取六水合硝酸锌1.66g、按照元素摩尔比为Zn：Co：Mn：Ti＝1:0.05:1：1称取六水合硝酸钴，0.5％wt硝酸锰水溶液，氯化钛配成混合液A，称取15.41g碳酸铵，溶解于100ml水中配成溶液B。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔比表面为316m2/g，微孔孔径分布在
Figure PCTCN2015092091-appb-000024
介孔比表面积为140m2/g，大孔比表面为99m2/g，介孔孔径大小分布在3-9nm。X射线衍射(XRD)表征显示，多组分金属复合物含Co2O3、Co3O4、MnO2、TiO2、ZnCo2O4、ZnMnO3和CHA结构的硅铝无机固体酸，金属氧化物晶粒大小9-18nm，无机固体酸晶粒大小为50-60nm；扫描电镜(SEM)表征表明，硅铝无机固体酸二次粒子大小为100-500μm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小9-18nm，二次粒子大小20-100nm；中强酸对应的NH3脱附峰温度为368℃，中强酸位点的量是2.3mol/kg。
将实施例17、18的催化剂在400℃，3.5MPa体积空速4000h-1的反应条件下，实施例17、18反应结果如下表。
Figure PCTCN2015092091-appb-000025
实施例19，将实施例17的催化剂在400℃，3.5MPa体积空速1500h-1的反应条件下，结果作为实施例19的反应结果列在下表。
实施例20，将实施例18的催化剂在400℃，3.5MPa体积空速1500h-1的反应条件下，结果作为实施例20的反应结果列在下表。
Figure PCTCN2015092091-appb-000026
对比例15，将实施例17的催化剂在400℃，3.5MPa体积空速300h-1的反应条件下，结果作为对比例15的反应结果列在下表。
对比例16，将实施例18的催化剂在400℃，3.5MPa体积空速300h-1的反应条件下，结果作为对比例16的反应结果列在下表。
Figure PCTCN2015092091-appb-000027
实施例17-20与对比例15-16，在不改变催化剂的前提下，只是改变了反应空速条件，其中实施例17-18的空速在权利要求的优选范围内，所以表现出了最高的低碳烯烃的选择性，而实施例19-20的空速虽然不在优选范围内，但属于权利要求的范围内所以仍有较高的低碳烯烃的选择性，而相对的对比例15-16，因为其反应空速不在权利要求范围内所以低碳烯烃选择性很低。
实施例21
化学复合法制备多组分金属复合物-多级孔结构的硅铝无机固体酸复合催化剂
以CaMnAl多组分金属复合物，多级孔结构的硅铝无机固体酸为例。
按氧化物SiO:Al2O3:Ca2O:R2O:H2O＝40:1:7:5:900(质量比)称取原料：硅溶胶30％(质量浓度)；硫酸铝；碳酸钙；N,N,N-一三甲基金刚烷氢氧化铵(R)；去离子水，室温混合后，在60℃下，200rpm速度搅拌24h后转移到水热釜中，155℃下晶化6天。自然冷却到室温，转移到烧杯中水浴70℃，按100ml原液：4g氯化铵的比例加入氯化铵，恒温搅拌3h，反复离心洗涤使得洗涤结束时上清液pH是7，沉淀物于120℃下烘干24h后，在650℃空气中焙烧3h得到多级孔结构的硅铝无机固体酸。
称取制备好的多级孔结构的硅铝无机固体酸，称取四水合硝酸锰1.49g，按照元素摩尔比为Mn：Ca:Al＝1:0.1:1称取无水硝酸钙，九水合硝酸铝，溶解于100ml水溶液中，通过浸渍法将CaMnAl引入到多级孔结构的硅铝无机固体酸上，并经过室温真空干燥，520℃静态空气中焙烧1.5h，得到Ca0.1Mn1Al1/mesoSiAl。多组分金属复合物的负载量为50wt％。根据此方法，可以改变各金属组分及其比例，以及多组分金属复合物的负载量。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，总比表面积565m2/g，其中微孔比表面占总比表面积的27％，微孔孔径分布在
Figure PCTCN2015092091-appb-000028
介孔比表面积占总比表面积57％，大孔比表面占总比表面积16％；介孔孔径大小分布在6-12nm。X射线衍射(XRD)表征显示，多组分金属复合物含CaO、MnO2、Al2O3、和具有CHA结构的硅铝无机固体酸，金属氧化物的晶粒大小5-13nm；无机固体酸晶粒大小为40-70nm；扫描电镜(SEM)表征表明，多级孔结构的硅铝无机固体酸二次粒子大小为10-100μm，无机固体酸晶粒大小为10-100nm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小5-13nm， 二次粒子大小15-50nm；中强酸对应的NH3脱附峰温度为370℃，中强酸位点的量是6mol/kg。
实施例22
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，称取并室温混合前驱体后，控制搅拌时间为18h后转移到水热釜中，170℃晶化5天。
获得的多级孔催化剂，总比表面积493m2/g，其中微孔比表面占总比表面积的24％，微孔孔径分布在
Figure PCTCN2015092091-appb-000029
介孔比表面积占总比表面积53％，大孔比表面占总比表面积23％；介孔孔径大小分布在5-11nm。中强酸对应的NH3脱附峰温度为392℃，中强酸位点的量是3.1mol/kg。
实施例23
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，称取并室温混合前驱体后，控制控制搅拌时间为3h后转移到水热釜中，165℃晶化5天又10h。最后在620℃焙烧80min。
获得的多级孔催化剂，总比表面积408m2/g，其中微孔比表面占总比表面积的16％，微孔孔径分布在
Figure PCTCN2015092091-appb-000030
介孔比表面积占总比表面积53％，大孔比表面占总比表面积31％；介孔孔径大小分布在5-13nm。中强酸对应的NH3脱附峰温度为389℃，中强酸位点的量是3.4mol/kg。
对比例17
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，称取并室温混合前驱体后，控制控制搅拌温度90时间为1h后转移到水热釜中，215℃晶化7天。最后在550℃焙烧4h。
获得的多级孔催化剂，总比表面积390m2/g，其中微孔比表面占总比表面积的66％，微孔孔径分布在
Figure PCTCN2015092091-appb-000031
介孔比表面积占总比表面积26％，大孔比表面占总比表面积8％；介孔孔径大小分布在2-4nm。中强酸对应的NH3脱附峰温度为403℃，中强酸位点的量是4.1mol/kg。
对比例18
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，称取并室温混合前驱体后，控制控制搅拌温度30时间为48h后转移到水热釜中，175℃晶化8天。最后在550℃焙烧3h。
获得的多级孔催化剂，总比表面积314m2/g，其中微孔比表面占总比表面积的81％，微孔孔径分布在
Figure PCTCN2015092091-appb-000032
介孔比表面积占总比表面积14％，大孔比表面占总比表面积5％；介孔孔径大小分布在2-4nm。中强酸对应的NH3脱附峰温度为368℃，中强酸位点的量是0.9mol/kg。
在375℃，3.7MPa体积空速6000h-1的反应条件下，反应结果如下表
Figure PCTCN2015092091-appb-000033
Figure PCTCN2015092091-appb-000034
实施例21-23与对比例17-18比较表现出了更优越的低碳烯烃的选择性，这是因为对比例17-18中三级孔道含量分布不符合权利要求的范围，而实施例22,23比实施例21有着更高的低碳烯烃的选择性，这是由于实施例21的大孔含量不在优选范围，且实施例22-23的三级孔含量不仅在优选范围更属于更优选的范围所以有着卓越的性能。
实施例24
化学复合法制备多组分金属复合物-多级孔结构的硅磷铝无机固体酸复合催化剂
按氧化物MgO：SiO2:Al2O3:H3PO4:R:H2O＝2：18:16:32:55:150(质量比)称取原料：白炭黑；硝酸铝；磷酸；TEAOH(R)；去离子水，室温混合后，在30℃下,500rpm速度搅拌10h后转移到水热釜中，200℃下晶化29h晶化中维持搅拌，搅拌速度100rpm。水浴骤冷到室温，反复离心洗涤使得洗涤结束时上清液pH是7，沉淀物于110℃下烘干24h后，在600℃空气中焙烧3h得到多级孔结构的硅磷铝无机固体酸。
使用上面方法制得的多级孔结构的硅磷铝无机固体酸，并称取四水合硝酸锰1.54g、按照元素摩尔比为Mn：Ca：Cr＝2：0.2:1称取氯化钙、九水合硝酸铬，溶解于水溶液中配成混合液A，其中无机固体酸与Cr质量比2:1，称取6.3g碳酸铵，溶解于100ml水中配成溶液B，50℃下将溶液B逐滴加入以7W功率tip超声，400rpm速度搅拌混合液A中，离心洗涤使得洗涤结束时上清液pH是7并经过110℃空气中干燥，500℃静态空气中焙烧1h，得到Ca0.2Mn2Cr1/MgSiPAl。然后，以此为载体，准确称取醋酸钯Co(Ac)2溶解在水中，通过浸渍引入到CaMnCr/MgSiPAl上，其中Co与Mn的摩尔比为0.01。根据此方法，可以改变各金属组分及其比例，以及多元金属复合物的负载量。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔孔径分布在
Figure PCTCN2015092091-appb-000035
介孔孔径大小分布在4-8nm，总的比表面积为416m2/g，其中微孔比表面积占57％，介孔比表面积占总比表面积的21％，大孔比表面占总面积22％，硅铝无机固体酸二次粒子大小为100-500μm,其晶粒大小为5-70nm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小0.5-16nm，二次粒子大小10-100nm,；中强酸对应的NH3脱附峰温度为371℃，中强酸位点的量是2.1mol/kg。
实施例25
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，称取并室温混合前驱体后，控制搅拌温度40℃，时间为2h后转移到水热釜中，180℃晶化2天。最后在流动空气下550℃焙烧4h。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔孔径分布在
Figure PCTCN2015092091-appb-000036
介孔孔径大小分布在5-9nm，总的比表面积为357m2/g，其中微孔比表面积占43％，介孔比表面积占总比表面积的30％，大孔比表面占总面积27％，硅铝无机固体酸二次粒子大小为50-150μm,其晶粒大小为20-80nm；高分辨透射电镜(HRTEM)表征表明，多组分金属复合物的晶粒大小1-13nm，二次粒子大小10-80nm；中强酸对应的NH3脱附峰温度为358℃，中强酸位点的量是1.9mol/kg。
实施例26
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，称取并室温混合前驱体后，控制搅拌温度为50℃，时间为1h后转移到水热釜中，165℃晶化5天又10h。最后在静态空气620℃焙烧2h。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔孔径分布在
Figure PCTCN2015092091-appb-000037
介孔孔径大小分布在4-9nm，总的比表面积为4415m2/g，其中微孔比表面积占33％，介孔比表面积占总比表面积的35％，大孔比表面占总面积32％，硅铝无机固体酸二次粒子大小为50-100μm,其晶粒大小为40-90nm；高分辨透射电镜(HRTEM)表征表明，多组分金属复 合物的晶粒大小3-6nm，二次粒子大小10-90nm；中强酸对应的NH3脱附峰温度为397℃，中强酸位点的量是2.7mol/kg。
对比例19
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，按氧化物MgO：SiO2:Al2O3:H3PO4:R:H2O:2：18:16:32:10:150(质量比)，称取原料称取并室温混合前驱体。控制晶化温度为150℃，时间24h。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔孔径分布在
Figure PCTCN2015092091-appb-000038
介孔孔径大小分布在4-9nm，总的比表面积为95m2/g，其中微孔比表面积占11％，介孔比表面积占总比表面积的55％，大孔比表面占总面积34％；中强酸对应的NH3脱附峰温度为320℃，中强酸位点的量是0.02mol/kg。
对比例20
催化剂制备过程与实施例21基本相同，不同之处在于制备多级孔结构的硅铝无机固体酸过程中，按氧化物MgO：SiO2:Al2O3:H3PO4:R:H2O:2：18:16:32:80:150(质量比)，称取原料称取并室温混合前驱体。控制晶化温度为180℃，时间72h。控制焙烧温度550℃，静态空气中，时间30min。
氮气物理吸脱附表征显示该催化剂具有多级孔结构，微孔孔径分布在
Figure PCTCN2015092091-appb-000039
介孔孔径大小分布在4-9nm，总的比表面积为69m2/g，其中微孔比表面积占14％，介孔比表面积占总比表面积的24％，大孔比表面占总面积62％；中强酸对应的NH3脱附峰温度为329℃，中强酸位点的量是0.03mol/kg。
在415℃，3.0MPa体积空速5000h-1的反应条件下，反应结果如下表
Figure PCTCN2015092091-appb-000040
实施例24-26所述的催化剂，多组分金属复合物及硅铝无机固体酸的晶粒及二次粒子的大小满足权利要求所述的范围，其比表面积满足权利要求的范围，并且形成了权利要求所述的三维三级孔道且三级孔道含量符合权利要求所述优选范围，其中实施例25-26在更优选范围，所以均表现出优异的性能。而对比例19-20虽然形成了三维三级孔道，但因为有机模板剂与水的比例不满足权利要求的范围，对比例19有机模板剂过少不利于形成足够的孔道结构，而对比例20有机模板剂过量，且焙烧时间不满足权利要求所述的时间范围，均导致了对比例19-20的比表面积低于权利要求的范围，从而表现为转化率很低，同时低碳烯烃的选择性也远低于本发明的催化剂。
实施例27
催化剂制备过程与实施例5基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将六水合硝酸铜用碳酸氢钠进行替换，保证替换金属的原子与被替换金属的原子为(1:10)，六水合硝酸钴用柠檬酸铁铵替换，保证替换金属的原子与被替换金属的原子为(1:2)。
实施例28
催化剂制备过程与实施例27基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将碳酸氢钠用碱式碳酸镁进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例29
催化剂制备过程与实施例27基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将碳酸氢钠用硝酸钾进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例30
催化剂制备过程与实施例27基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将碳酸氢钠用硝酸铯进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例31
催化剂制备过程与实施例27基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将碳酸氢钠用硝酸镧进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例32
催化剂制备过程与实施例5基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将六水合硝酸铜用25wt.％硝酸锰进行替换，保证替换金属的与被替换金属的原子为(1:1)，六水合硝酸钴用柠檬酸铁铵替换，保证替换金属的原子与被替换金属的原子为(1:2)，γ-Al2O3用硝酸镓替换保证替换金属的原子与被替换金属的原子为(1:1)。
实施例33
催化剂制备过程与实施例32基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将硝酸镓用硝酸锗进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例34
催化剂制备过程与实施例32基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将硝酸镓用硝酸锆进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例35
催化剂制备过程与实施例32基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将硝酸镓用硝酸铟进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
实施例36-40
催化剂制备过程与实施例27-31基本相同，不同之处在于更换了多元金属复合物中的金属元素，在配置金属前驱体溶液时将硝酸锌用25wt.％硝酸锰进行替换，保证替换金属的原子与被替换金属的原子为(1:1)。
在400℃，3.0MPa体积空速6000h-1的反应条件下，反应结果如下表。
Figure PCTCN2015092091-appb-000041
对比例21
作为对比例21，商品Na-ZSM-5分子筛与共沉淀法制备的Co0.1Cr3Zn2的复合氧化物机械混合得到的混合物作为催化剂，在相同条件下，低碳烷烃及烯烃的选择性不超过20％，产生大量甲烷而且催化剂的稳定性极差，15小时随即失活。这是由于该分子筛仅含微孔结构，不具有介孔结构，反应生成的积碳极易堵塞微孔，从而导致失活。
对比例22
作为对比例22，用于甲醇合成的商品CuZnAl催化剂与不具备多级孔结构的商品MTO催化剂SAPO-34，按照质量比1:1，进行机械混合，在相同条件下反应。只能得到烷烃，几乎没有烯烃生成。这是因为商品SAPO-34分子筛不具备权利要求所述的多级孔结构，不利于传质，导致产物过度加氢，使得产物中几乎没有烯烃产生。
对比例23
以碳纳米管为载体，管腔内负载FeN纳米颗粒，可以限制纳米粒子的聚集长大，避免失活，经过K和Mn促进，得到K0.4Mn1.0FeN@CNTs，可以选择性生成低碳烯烃。在300℃，5bar，空速15000h-1，H2/CO/Ar＝47.5/47.4/5.1的条件下，转化率为11.9％，C2 ＝-C4 ＝的选择性为43.6％。在该催化剂表面，CO解离生成的表面碳物种，与解离的氢原子反应生成CHx中间物种，在表面上进一步相互偶联，生成不同碳链长度的碳氢化合物或者加氢生成烷烃，因此产物众多，产物符合ASF分布。
在400℃，2MPa体积空速4000h-1的反应条件下，对比例21、22反应结果如下表。
在300℃，0.5MPa体积空速15000h-1的反应条件下，对比例23反应结果如下表。
Figure PCTCN2015092091-appb-000043
Figure PCTCN2015092091-appb-000044
实施例1-40所述催化剂的反应产物中产物中C2-C4在总烃产物中的选择性可达60～95％，低碳烯烃在总烃产物中的选择性高达50～85％，由于催化剂金属复合物表面不活化氢分子，避免了甲烷的大量生成，甲烷选择性和C5+长碳链碳氢化合物的选择性可以极低，两者小于10％。无机固体酸的多级孔结构避免催化剂失活，连续反应100小时CO的转化率稳定，产物选择性稳定。
实施例1-40中催化剂的性能明显优于传统改进的费托催化剂，以及传统MTO反应催化剂与甲醇合成催化剂机械混合得到的催化剂。原因是由于本发明的催化剂金属复合物表面经过含氢气或一氧化碳的气氛还原活化之后，在表面结构中形成氧空位，即氧为配位不饱和状态，可高效地催化活化CO生成中间态物种CHx(其中x＝1,2,3)中的一种或两种以上的物种，表面氧物种与CO反应生成CO2，这些极其活泼的CHx物种与CO结合生成CHxCO，避免了甲烷的大量生成，甲烷选择性和C5+长碳链碳氢化合物的选择性极低，两者共为5～10％。同时生成的中间态物种在表面为弱吸附，极易从表面脱附并扩散至无机固体酸的孔道内，被酸性位进一步催化转化反应生成低碳烃。本发明的无机固体酸具有多级孔结构，从而避免催化剂失活，连续反应100小时CO的转化率稳定，产物选择性稳定。而传统微孔MTO分子筛催化剂不具备多级孔结构，很容易被反应生成的中间物种堵塞导致催化剂快速失活，且不利于传质直接混合使用只能得到烷烃，几乎没有烯烃产生。相比之下，Fe为主成分的催化剂仍遵循费托反应机理，即CO在催化剂表面解离吸附，生成表面碳和表面氧，表面氧与吸附态的氢反应生成水，表面碳则与表面氢反应生成CHx，CHx在表面吸附较强，多个表面CHx聚合，发生链增长，由催化剂表面性质决定形成不同碳链长度的碳氢化合物并脱附至气相。
本发明所提供的催化剂为复合材料，其有效成分包括多组分金属复合物和多级孔结构的无机固体酸，可以催化合成气转化生成C2-C4低碳烃，CO单程转化率为10～60％，低碳烃在所有碳氢化合物产品中的选择性可高达60～95％，其中低碳烯烃(C2 ＝-C4 ＝)的选择性为50～85％。该方法具有工艺简单，设备投资少的特点，具有重要的应用前景。

Claims (12)

  1. 一种催化剂，其特性在于：
    所述催化剂为多组分金属复合物和多级孔结构的无机固体酸构成的复合材料；无机固体酸具有微孔、介孔和大孔的多级孔结构；金属复合物分散在无机固体酸表面或孔道中；
    按催化剂的总质量为100％计，所述多组分金属复合物在整个催化剂中的含量为10wt.％～75wt.％，优选25wt.％-75wt.％；
    所述多级孔结构的无机固体酸是由无机固体酸二次粒子组成，无机固体酸二次粒子大小为100nm-500μm，优选为150nm-100μm；
    所述无机固体酸二次粒子是由大小为5-200nm(优选20-120nm)的无机固体酸晶粒堆积形成的；
    所述无机固体酸二次粒子具有三维三级孔道结构，包括一级孔，二级孔，三级孔三种孔道；
    所述一级孔是孔道直径小于2nm范围的微孔孔道，微孔位于无机固体酸晶粒内部；
    所述二级孔是孔道直径2nm-50nm的介孔孔道，优选为2-15nm，二级孔是由无机固体酸晶粒堆积而成，位于无机固体酸二次粒子内部及三级孔的孔壁上；
    所述三级孔是孔道直径分布大于50nm的大孔孔道，是无机固体酸二次粒子堆积而成；
    所述三种孔道之间相互连接贯通，构成三维三级孔道结构，二级孔可位于相邻三级孔孔壁，一级孔可位于相邻的二级孔和/或三级孔孔壁；
    所述的多级孔结构的无机固体酸由N2物理吸附测定的BET比表面积为100～1200m2/g，孔容为0.25～0.80ml/g；按照比表面积计算，微孔占10-65％，介孔占20-75％，大孔占15-70％；优选的微孔的比表面积占10-60％，介孔比表面积占20-70％，大孔占20-70％；更优选为微孔的比表面积占10-50％，介孔比表面积占总比表面积的30-70％，大孔占20-60％。
  2. 按照权利要求1所述的催化剂，其特征在于：
    所述的多组分金属复合物中的金属为两种或三种以上的金属元素，优选为两种至五种金属元素；所述金属复合物包括金属氧化物以及金属、金属碳化物、金属氮化物、和金属无机酸盐中的一种或二种以上；
    所述金属元素包括必要金属元素以及其它元素，其中必要金属元素为Zn或Co或Cr或Mn；
    若所述必要金属元素为Zn，则其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Co、Cu、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Cr、Mn、Co、Cu、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Cr、Mn、Co、Cu、Pd、Ce中的一种或二种以上；
    若所述必要金属元素为Co时，其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Cr、Mn、Cu、Zn、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Cr、Mn、Cu、Zn、Pd、Ce中的一种或二种以上；
    若所述必要金属元素为Cr，则其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Mn、Fe、Co、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Mn、Co、Cu、Zn、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Mn、Co、Cu、Zn、Pd、Ce中的一种或二种以上；
    若所述必要金属元素为Mn，则其它元素为Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、Cr、Fe、Co、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、In、Sn、Cs、La、Ce中的一种或二种以上；其它元素优选为Al、K、Ti、V、Cr、Co、Cu、Zn、In、La、Mo、Ce、Pd中的一种或二种以上，其它元素更优选为Al、Ti、Cr、Co、Cu、Zn、Pd、Ce中的一种或二种以上；
    所述的多组分金属复合物中，金属氧化物的含量为5～90％，金属和金属碳化物和金属氮化物中的一种或两种以上的总质量含量可以是小于或者等于10％，金属无机酸盐的含量为10～95％；优选金属氧化物的含量为30-90％，金属和金属碳化物和金属氮化物中的一种或两种以上的总质量含量小于5％，金属无机酸盐的含量为10-70％；
    所述的多组分金属复合物中必要元素Zn或Co或Cr或Mn与其他元素的总摩尔比为(0.1～5.0)：1，优选摩尔比为0.2～3.5；
    所述无机酸盐是由阳离子与阴离子组成，其中Li、Na、Mg、Al、K、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Co、Cu、Zn、Ga、Ge、Zr、Mo、Pd、Ag、Cd、Sn、Cs、Ce中的一种或二种以上可以以阳离子形式存在，而Al、Si、V、Cr、Mn、Fe、Co、Zn、Mo、Ti、Zr、Ce、Ga、In、Ge也可以以ZnO2 2-、Al2O4 2-、SiO3 2-、SiO4 4-、TiO3 2-、TiO3 3-、VO3 -、VO3 2-、CrO4 2-、Cr2O4 2-、Mn2O4 2-、Fe2O4 2-、Co2O4 2-、Ni2O4 2-、Fe(CN)6 3-、Fe(CN)6 4-、MoO4 2-、TiO3 2-、ZrO3 2-、CeO3 2-、Ga2O4 2-、In2O4 2-、GeO3 2-、GeO4 4-、SrO3 4-中的一种或二种以上阴离子形式存在，阳离子与阴离子组成无机酸盐，无机酸盐组成如表1所列；且构成阳离子和构成阴离子的金属元素不同。
  3. 按照权利要求2所述的催化剂，其特征在于：
    所述金属复合物是由权利要求2中所述金属、金属碳化物、金属氮化物中的一种或两种以上，以及金属氧化物、金属无机酸盐的晶粒相互均匀分散形成，其晶粒大小为0.5-20nm，优选1-10nm；同时这些晶粒进一步堆积形成二次粒子，二次粒子大小为10nm-200μm，二次粒子中晶粒堆积形成的孔道直径为2-20nm，优选为5-15nm。
  4. 按照权利要求1所述的催化剂，其特征在于：
    所述的无机固体酸由H、O为必要元素，以及Al、Si、P、Zr、Ti、Ge中的一种或两种以上元素组成，形成由硅氧氢元素组成的无机固体酸、由硅铝氧氢元素组成的无机固体酸、由硅铝磷氧氢元素组成的无机固体酸、由钛硅氧氢元素组成的无机固体酸、由锆硅氧氢元素组成的无机固体酸、由锗硅氧氢元素组成的无机固体酸、由锗铝磷氧氢元素组成的无机固体酸中的一种或二种以上。
  5. 按照权利要求1、3或4所述的催化剂，其特征在于：
    所述的多级孔结构的无机固体酸具有酸性特征；
    所述的酸性位分布于权利要求1所述的三维三级孔道；
    按照NH3-TPD定义酸性强弱，所述固体无机酸包含弱酸、中强酸、强酸三种酸性；
    该NH3-TPD是根据NH3的脱附峰位置，所述脱附峰的位置是指在标准测试条件下，在样品质量w与载气流速f比值(w/f)＝100g·h/L，10℃/min升温速度的测试条件下，TCD记录脱附NH3的热导信号，绘制脱附曲线，根据曲线峰位置顶点将所述无机固体分为三种酸性强度；
    所述弱酸是NH3脱附温度小于275℃的酸性位；
    所述中强酸是NH3脱附温度在275-500℃的酸性位；
    所述强酸是NH3脱附温度大于500℃的酸性位；
    所述无机固体酸中，中强酸位点的量是0.06-10mol/kg；优选1-10mol/kg；
    所述的多组分金属复合物和多级孔结构的无机固体酸构成复合材料；多组分金属复合物中尺寸在0.5-10nm的粒子可以位于多级孔结构的无机固体酸的微孔、介孔或者大 孔孔道内以及无机固体酸外表面，多组分金属复合物中尺寸在10-200nm的二次粒子可以位于多级孔结构的无机固体酸的大孔和介孔的孔道内或者无机固体酸外表面，尺寸大于200nm的金属复合物二次粒子分散在多级孔结构的无机固体酸外表面，多组分金属复合物的外表面与无机固体酸的大孔和介孔的内表面及无机固体酸二次粒子的外表面堆积形成活性孔；所述活性孔连接金属复合物介孔与多级孔结构的无机固体酸中的三维三级孔道，使得所有孔道连通复合。
  6. 按照权利要求1或5所述的催化剂，其特征在于：
    所述的多级孔结构的无机固体酸制备方法包括软模板水热法、硬模板水热法或结晶控制水热法；在软模板水热法、硬模板水热法或结晶控制水热法的老化操作中，使用恒温搅拌老化处理有利于形成多级孔结构的无机固体酸；
    所述结晶控制水热法，快速老化，并在晶化过程中控制搅拌速率和温度，避免分子筛晶粒过度长大，促进小晶粒的形成，使更多的小晶粒之间产生晶间介孔，获得多级孔结构的无机固体酸，同时通过调变老化及晶化条件可以同时调变权利要求5所述的酸性强弱及中强酸的量；具体步骤包括：均匀溶胶分散液的制备、老化、晶化、洗涤、干燥和焙烧；所述的均匀溶胶分散液的制备是将无机固体酸所含有元素的前驱体按所需比例，称量后投入含有水的容器中，在室温下进行搅拌分散，同时加入有机微孔模板剂制得液相分散体系；所述老化方法是将配制好的液相分散体系在温度控制在20-60℃，时间10min-24h，搅拌速率50-1000rpm；晶化过程中搅拌速率50-500rpm，温度120-250℃，时间12h-10day；洗涤方法可以是过滤洗涤或离心洗涤，过滤洗涤应保证洗涤结束时滤液pH是6.5-7.5，离心洗涤应保证洗涤结束时上清液是6.5-7.5；所述干燥过程，温度在100-150℃，时间大于12h；所述焙烧过程，温度在500-650℃，时间1-8h；
    所述软模板水热法，是利用有机介孔模板剂，使用水热法合成多级孔结构的无机固体酸，具体步骤涉及均匀溶胶分散液的制备，老化，晶化，洗涤，干燥和焙烧；所述的均匀溶胶分散液的制备是将无机固体酸所含有元素的前驱体按所需质量比，称量后投入含有水的容器中，在室温下进行搅拌分散，同时加入有机微孔模板剂及有机介孔模板剂(其质量比为0.3～0.8)，制得液相分散体系，老化过程中温度控制在20-60℃，时间10min-24h，搅拌速率50-1000rpm；晶化过程中搅拌速率50-500rpm，温度120-250℃，时间12h-10day；洗涤方法可以是过滤洗涤或离心洗涤，过滤洗涤应保证洗涤结束时滤液pH是6.5-7.5，离心洗涤应保证洗涤结束时上清液是6.5-7.5；所述干燥过程，温度在100-150℃，时间大于12h；所述焙烧过程，温度在500-650℃，时间1-8h；
    所述硬模版水热法，是可以在650℃下被氧化的纳米碳材料、SBA系列、M41S系列、HMS系列、MSU系列、KIT系列、FDU系列、AMS系列、HOM系列、MCM-41介孔分子筛中的一种或两种以上作为硬模板，使用水热法合成多级孔结构的无机固体酸，具体步骤涉及均匀溶胶分散液的制备，老化，晶化，洗涤，干燥和焙烧；所述的均匀溶胶分散液的制备是将无机固体酸所含有元素的前驱体按所需质量比，称量后投入含有水的容器中进行搅拌分散，同时加入有机微孔模板剂及硬模板材料(其质量比例为0.3～0.8)制得液相分散体系，抑制晶粒长大，促进小晶粒形成介孔；温度控制在20-60℃，时间10min-24h，搅拌速率50-1000rpm；晶化过程中搅拌速率50-500rpm，温度120-250℃，时间12h-10day，洗涤方法可以是过滤洗涤或离心洗涤，过滤洗涤应保证洗涤结束时滤液pH是6.5-7.5，离心洗涤应保证洗涤结束时上清液是6.5-7.5；所述干燥过程，温度在100-150℃，时间大于12h；所述焙烧过程，温度在500-700℃，时间1-8h；
    所述均匀溶胶分散液中前驱体是水玻璃、硅溶胶、超微SiO2、白炭黑、硅酸钠、TMOS、硅酸酯、四氯化硅、高岭土、硝酸铝、硫酸铝、铝酸钠、薄水铝石、拟薄水铝石、三水铝石、三水异丙醇铝、三氯化铝、氢氧化铝、烷氧基铝、超微粉末铝、氧化铝、磷酸、 磷酸铝、磷酸钠、氧化锆、硝酸锆、磷酸锆、硅酸锆、四氯化钛、钛酸丁酯、氧化钛、氧化锗、硝酸锗、氯化锗、三氯甲基锗、四乙基锗中的一种或两种以上；
    所述有机微孔模板剂是TMA、TPA、TEA、TEAOH、DDO、TBA、TQA、乙二胺、吡咯烷、胆碱、PDN、RDN、PDA、季戊四醇、羟酸、丙基硫醛、三丙胺、DABCO、二正丙胺、叔丁胺、异丙胺、奎宁环、新戊胺、三乙醇胺、二环己胺、N,N-二甲基苄胺、N,N-二甲基醇胺、N,N-二乙基乙醇胺、2-甲基吡啶、哌啶、吗啡中的一种或两种以上；
    所述有机介孔模板剂是CTBA、CTBABr、十二烷基磷酸酯、长链伯胺、聚氧乙烯、聚氧丙烯、聚氧乙烯嵌段醚共聚物、P123、明胶与戊二醛交联物、TPHAC中的一种或两种以上；
    所述溶胶前驱体和有机模板剂(包括有机微孔模板剂和有机介孔模板剂)以及水的质量比为，溶胶前驱体：有机模板剂：水＝(20-65)：(15-50)：100。
  7. 按照权利要求1所述的催化剂，其特征在于：
    所述催化剂中多组分金属复合物和多级孔结构的无机固体酸的复合方式包括包覆生长法，超声辅助的化学复合法，或物理复合法；
    所述的包覆生长法，是在多组分金属复合物上，通过权利要求6所述的方法，在多组分金属复合物表面生长出一层覆盖率至少80％以上或者完全覆盖的多级孔结构的无机固体酸，即先制备均匀溶胶分散液，再将多组分金属复合物分散于均匀溶胶分散液中，再经过老化、晶化、洗涤，干燥和焙烧得到包覆有多级孔结构的无机固体酸的多组分金属复合物；多组分金属复合物中，由Mg、Al、Ca、Sr、Ba、Ti、V、Cr、Mn、Fe、Co、Cu、Zn、Zr、Mo、Pd、Ag、Cd、In、Sn、La、Ce元素组成的金属氧化物和无机酸盐由共沉淀法、浸渍法、或超声离子交换法制备；由Li、Na、K、Ga、Ge、Cs元素组成的金属氧化物和无机酸盐由浸渍法、或超声离子交换法制备；Al、Fe、Co、Cu、Zn、Mo、Pd元素还可采用化学气相沉积法或者浸渍法制备；
    所述的超声辅助的化学复合法，是在多级孔结构的无机固体酸上通过超声共沉淀法，化学气相沉积法或超声离子交换法引入多组分金属复合物复合得到；
    所述的物理复合法，是通过球磨，机械混匀法，摇床，振荡混合的机械化学法对多级孔结构的无机固体酸和多组分金属复合物进行复合。
  8. 按照权利要求7所述的催化剂，其特征在于：
    所述的超声共沉淀法，指将多组分金属复合物所需两种或三种以上的金属前驱体溶解于溶剂中，得到两种或三种以上的金属阳离子溶液，然后将多级孔结构的无机固体酸在超声搅拌条件下加入到上述溶液中，超声方法可以是bath超声或Tip超声，超声功率为1-20W/(ml样品)，频率40KHz-80MHz，沉淀温度2℃-80℃，时间2min-2h，搅拌速率50-1000rpm，混合均匀之后，按所需质量比加入沉淀剂，得到均匀的沉淀物，再经干燥、焙烧，干燥温度是80-150℃，时间大于12h，焙烧温度是300-650℃，时间1-3h；
    所述超声共沉淀法中，金属前驱体选自硝酸盐、甲酸盐、醋酸盐、卤化物、羰基化合物、C1～C5有机酸盐中的一种或两种以上；沉淀剂选自碳酸铵、碳酸氢铵、碳酸锂、碳酸氢锂、碳酸钠、碳酸氢钠、碳酸钾、碳酸氢钾、碳酸镁或草酸中的一种或两种以上，优选为碳酸铵、碳酸氢铵、碳酸氢钠、碳酸氢钾，最佳为碳酸铵、碳酸氢铵、碳酸氢钠；沉淀温度控制在2～80℃的范围内，干燥温度为80～150℃，时间大于12h，焙烧温度为300～650℃，时间1-3h，焙烧气氛可以是流动的空气或者静置空气；
    所述超声离子交换法是指将多组分金属复合物所需两种或三种以上的金属前驱体溶解于溶剂中，得到两种或三种以上的金属阳离子溶液，然后将多级孔结构的无机固体酸在超声搅拌条件下加入到上述溶液中，超声方法可以是bath超声或Tip超声，超声功率为1-20W/(ml样品)，频率40KHz-80MHz，沉淀温度2℃-60℃，时间1h-12h，搅拌 速率50-500rpm，再经过洗涤、干燥、焙烧，洗涤方法可以是过滤洗涤或离心洗涤，使洗涤后pH在6.5-7.5，干燥温度是80-150℃，时间大于12h，焙烧温度是300-650℃，时间1-3h；
    所述物理复合中的球磨法，温度为25～100℃，载气为：a)氮气和/或惰性气体，b)氢气与氮气和/或惰性气体的混合气，其中氢气于混合气中的体积为5～50％，c)CO与氮气和/或惰性气体的混合气，其中CO于混合气中的体积为5～20％，或d)O2与氮气和/或惰性气体的混合气，其中O2于混合气中的体积为5-20％，所述惰性气体为氦气、氩气、氖气中的一种或两种以上；
    所述物理复合中的机械混匀法，是指使用包括3D旋转混匀仪、行星式混匀仪、或涡轮混匀仪等混匀装置，将多组分金属复合物和多级孔结构的无机固体酸加入容器中，利用这些物料及容器的高速运动产生的挤压力、撞击力、裁剪力、摩擦力等中的一种或两种以上作用实现分离、破碎、混匀等目的，通过调变温度与载气气氛实现机械能、热能与化学能的转换，进一步增强不同组分间的相互作用；反应过程中，设置温度20-100℃，载气气氛为：a)氮气和/或惰性气体，b)氢气与氮气和/或惰性气体的混合气，其中氢气于混合气中的体积为5～50％，c)CO与氮气和/或惰性气体的混合气，其中CO于混合气中的体积为5～20％，d)O2与氮气和/或惰性气体的混合气，其中O2于混合气中的体积为5-20％，所述惰性气体为氦气、氩气、氖气中的一种或两种以上。
  9. 一种使用权利要求1-8任一所述的催化剂由合成气一步法直接制备低碳烯烃的方法，其特征在于：
    使用权利要求1-8任一所述催化剂进行催化反应，在所需反应温度、反应压力条件下，反应原料气体H2/CO体积比＝0.5/1～4/1，制备C2-C4低碳烯烃，即含有两个碳原子至四个碳原子数的烯烃，包括乙烯、丙烯和丁烯中的一种或者一种以上。
  10. 按照权利要求9所述的方法，其特征在于：
    所述催化反应，进行该反应前，包括一个催化剂预处理过程，预处理气氛为a)H2和CO的混合气，其中H2/CO体积比为0.5/1～4/1；
    或，b)氢气与惰性气体的混合气；b)中，氢气在混合气中的体积百分比为5～100％，惰性气体为氮气、氦气、氩气或氖气中的一种或两种以上；
    或，c)CO与惰性气体的混合气；c)中，CO在混合气中的体积百分比为5～100％，惰性气体为氮气、氦气、氩气或氖气中的一种或两种以上；
    所述催化剂预处理的温度为250～600℃，预处理压力为0.1～3.0MPa，预处理的空速为500～5000h-1，空速优选为1000～4000h-1；
    所述金属复合物经过含氢气或一氧化碳的气氛还原活化之后，表面结构中具有氧空位，即氧为配位不饱和状态，可高效地催化活化CO生成中间态物种CHx(其中x＝1,2或3)中的一种或两种以上的物种，表面氧物种与CO反应生成CO2，这些极其活泼的CHx物种与CO结合生成CHxCO，生成的中间态物种在表面为弱吸附，极易从表面脱附并扩散至无机固体酸的孔道内，被进一步催化转化反应生成低碳烃，无机固体酸的孔道大小和酸性可以调变低碳烃的选择性以及其中烯烃和烷烃的相对比例。
  11. 按照权利要求9所述的方法，其特征在于：
    所述反应原料气体为混合气，混合气中含有H2、CO、以及其他气体，其他气体为惰性气体和/或非惰性气体中的一种或者两种；
    所述惰性气体为氮气、氦气、氩气、氖气中的一种或两种以上，在反应原料气体中的体积含量小于10％；
    所述非惰性气体为二氧化碳、气化的水、甲醇、乙醇中的一种或者两种，在反应原料气体中的体积含量小于50％；
    H2与CO的体积比H2/CO为0.5/1～4/1。
  12. 按照权利要求9或11所述的方法，其特征在于：
    所述反应采用的装置为流化床、移动床或固定床；
    所述反应温度为300～500℃，反应温度优选为350～450℃，空速为500～10000h-1，空速优选为2000～7000h-1；
    所述反应为连续流动反应模式或间歇反应模式；
    所述连续流动反应模式中，反应压力为0.1～6.0MPa，反应压力优选为1.0～5.0MPa；
    所述间歇反应模式中，反应压力为1.0～10MPa，反应压力优选为1.0～5.0MPa。
PCT/CN2015/092091 2015-07-02 2015-10-16 一种催化剂及由合成气一步法直接制备低碳烯烃的方法 Ceased WO2017000427A1 (zh)

Priority Applications (6)

Application Number Priority Date Filing Date Title
EP15896956.8A EP3318327A4 (en) 2015-07-02 2015-10-16 CATALYST AND METHOD FOR THE PRODUCTION OF LIGHT OLEFINS DIRECTLY FROM SYNTHESEGAS BY A UNIVERSAL PROCESS
JP2017567812A JP6666365B2 (ja) 2015-07-02 2015-10-16 一段階法によって合成ガスから軽質オレフィンを直接調製する触媒及び方法
RU2018103755A RU2706241C2 (ru) 2015-07-02 2015-10-16 Катализатор и способ получения легких олефинов непосредственно из синтез-газа в результате осуществления одностадийного технологического процесса
US15/740,653 US10532961B2 (en) 2015-07-02 2015-10-16 Catalyst and method of preparing light olefin directly from synthesis gas by one-step process
ZA2017/08553A ZA201708553B (en) 2015-07-02 2017-12-15 Catalyst and method of preparing light olefin directly from synthesis gas by one-step process
SA517390644A SA517390644B1 (ar) 2015-07-02 2017-12-28 محفز وطريقة لتحضير الأولفينات الخفيفة مباشرة من غاز التخليق بعملية من خطوة واحدة

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201510387209.2 2015-07-02
CN201510387209 2015-07-02

Publications (1)

Publication Number Publication Date
WO2017000427A1 true WO2017000427A1 (zh) 2017-01-05

Family

ID=57607570

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2015/092091 Ceased WO2017000427A1 (zh) 2015-07-02 2015-10-16 一种催化剂及由合成气一步法直接制备低碳烯烃的方法

Country Status (8)

Country Link
US (1) US10532961B2 (zh)
EP (1) EP3318327A4 (zh)
JP (1) JP6666365B2 (zh)
CN (1) CN106311317B (zh)
RU (1) RU2706241C2 (zh)
SA (1) SA517390644B1 (zh)
WO (1) WO2017000427A1 (zh)
ZA (1) ZA201708553B (zh)

Cited By (47)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106984303A (zh) * 2017-04-28 2017-07-28 武汉理工大学 一种担载贵金属的等级孔大孔‑介孔γ‑Al2O3催化剂及其制备方法
WO2018221706A1 (ja) * 2017-05-31 2018-12-06 古河電気工業株式会社 メタノール改質触媒構造体、メタノール改質用装置、メタノール改質触媒構造体の製造方法及びオレフィンまたは芳香族炭化水素の少なくとも一方の製造方法
CN109289865A (zh) * 2018-09-30 2019-02-01 中国科学院山西煤炭化学研究所 一种合成气制低碳混合醇的含硅催化剂及制法和应用
CN109304220A (zh) * 2017-07-28 2019-02-05 中国石油化工股份有限公司 合成气制备低碳烯烃的催化剂
WO2019030279A1 (en) * 2017-08-08 2019-02-14 Basf Se COMPOSITION COMPRISING A MIXED METAL OXIDE AND A MOLDING COMPRISING A ZEOLITHIC MATERIAL HAVING A TYPE OF CHA STRUCTURE AND AN ALKALINE-EARTH METAL
CN109331863A (zh) * 2018-07-02 2019-02-15 山东科技大学 一种原位掺碳型镍基介孔催化剂的制备和应用
JP2019038777A (ja) * 2017-08-25 2019-03-14 国立大学法人富山大学 低級オレフィンの製造方法
CN109651030A (zh) * 2017-10-10 2019-04-19 中国石油化工股份有限公司 合成气直接制备低碳烯烃的方法
CN109701601A (zh) * 2017-10-26 2019-05-03 中国石油化工股份有限公司 组合催化剂体系及其用途
CN109701596A (zh) * 2017-10-26 2019-05-03 中国石油化工股份有限公司 催化剂体系
CN109847791A (zh) * 2017-11-30 2019-06-07 中国科学院大连化学物理研究所 一种催化剂、其制备方法及在丁烯歧化反应中的应用
CN110229380A (zh) * 2019-07-08 2019-09-13 福建远翔新材料股份有限公司 一种高效、高透明二氧化硅塑料薄膜开口剂的制备方法
CN110474060A (zh) * 2019-07-01 2019-11-19 吉林大学 一种高效三维网状氮自掺杂碳气凝胶的制备方法及氧还原催化剂应用
CN110691646A (zh) * 2017-05-31 2020-01-14 古河电气工业株式会社 Co变换或逆变换催化剂结构体及其制造方法、co变换或逆变换反应装置、二氧化碳和氢的制造方法、以及一氧化碳和水的制造方法
CN111111760A (zh) * 2018-10-30 2020-05-08 中国石油化工股份有限公司 二氧化碳加氢制取低碳烯烃的催化剂及其用途
CN111111764A (zh) * 2018-10-30 2020-05-08 中国石油化工股份有限公司 催化剂体系及其用途
CN111195521A (zh) * 2020-01-15 2020-05-26 大连凯信科技研发有限公司 烯烃催化剂及其制备方法以及在合成气制烯烃中的应用
CN111519073A (zh) * 2020-06-03 2020-08-11 上海鑫烯复合材料工程技术中心有限公司 一种具有三峰特征的纳米增强金属基复合材料
CN111644169A (zh) * 2020-06-17 2020-09-11 宁夏大学 金属复合改性纳米氧化锆催化剂及其制备方法和应用
EP3593901A4 (en) * 2016-12-30 2020-11-04 Shanghai Advanced Research Institute, Chinese Academy of Sciences CATALYST FOR THE PREPARATION OF HYDROCARBONS FROM CARBON DIOXIDE BY ONE-STEP HYDROGENATION AND ITS PREPARATION PROCESS
CN112108180A (zh) * 2019-06-21 2020-12-22 中国科学院大连化学物理研究所 一种合成气直接转化制低碳烯烃的催化剂及其制备方法
EP3632557A4 (en) * 2017-06-02 2021-01-20 Dalian Institute Of Chemical Physics Chinese Academy of Sciences CATALYST AND METHOD FOR DIRECT CONVERSION OF SYNTHESIS GAS FOR THE PRODUCTION OF LIGHT OLEFINS
CN112705218A (zh) * 2019-10-24 2021-04-27 中国石油化工股份有限公司 合成气制低碳烯烃的催化剂、制备方法及其应用
JP2021516147A (ja) * 2018-01-26 2021-07-01 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ 有機アルカリで修飾された複合触媒及び一酸化炭素の水素化によるエチレンの製造方法
JP2021516146A (ja) * 2018-01-26 2021-07-01 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ 触媒及び合成ガスの直接転化による低級オレフィンの製造方法
US20210268482A1 (en) * 2018-06-29 2021-09-02 Dow Global Technologies Llc Hybrid catalysts comprising a zeolite and a mixed metal oxide component for converting syngas into c2 and c3 olefins
CN113385191A (zh) * 2020-03-13 2021-09-14 湘潭大学 无机固体硅基磺酸和/或磷酸催化剂及其制备方法和应用
US11161101B2 (en) 2017-05-31 2021-11-02 Furukawa Electric Co., Ltd. Catalyst structure and method for producing the catalyst structure
EP3744426A4 (en) * 2018-01-26 2021-11-03 Dalian Institute of Chemical Physics, Chinese Academy of Sciences CATALYST WITH LF TYPE B ACID AND PROCESS FOR THE DIRECT CONVERSION OF SYNTHESIS GAS INTO ETHYLENE
EP3744425A4 (en) * 2018-01-26 2021-11-03 Dalian Institute of Chemical Physics, Chinese Academy of Sciences SUPPORTED CATALYST AND METHOD FOR DIRECT CONVERSION OF SYNTHESIS GAS TO LOW CARBON OLEFINE
CN113600214A (zh) * 2021-09-02 2021-11-05 广州大学 一种核壳型Fe2O3@TixOy-Pz光催化剂的制备方法及应用
US11547987B2 (en) 2017-05-31 2023-01-10 Furukawa Electric Co., Ltd. Structured catalyst for oxidation for exhaust gas purification, method for producing same, automobile exhaust gas treatment device, catalytic molding, and gas purification method
CN116020435A (zh) * 2021-10-27 2023-04-28 中国石油化工股份有限公司 贵金属负载铟锆碳复合材料及其制备方法和二氧化碳加氢制备甲醇的方法
CN116060113A (zh) * 2021-10-29 2023-05-05 中国石油化工股份有限公司 一种直馏柴油加氢改质催化剂及其制备方法和应用
US11648538B2 (en) 2017-05-31 2023-05-16 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US11648543B2 (en) 2017-05-31 2023-05-16 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US11648542B2 (en) 2017-05-31 2023-05-16 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US11655157B2 (en) 2017-05-31 2023-05-23 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US11654422B2 (en) 2017-05-31 2023-05-23 Furukawa Electric Co., Ltd. Structured catalyst for catalytic cracking or hydrodesulfurization, catalytic cracking apparatus and hydrodesulfurization apparatus including the structured catalyst, and method for producing structured catalyst for catalytic cracking or hydrodesulfurization
US11680211B2 (en) 2017-05-31 2023-06-20 Furukawa Electric Co., Ltd. Structured catalyst for hydrodesulfurization, hydrodesulfurization device including the structured catalyst, and method for producing structured catalyst for hydrodesulfurization
CN116285128A (zh) * 2023-04-23 2023-06-23 罗孚橡胶（江苏）有限公司 一种高强度耐老化橡胶及其制备方法
US12030041B2 (en) 2017-05-31 2024-07-09 Furukawa Electric Co., Ltd. Structured catalyst for steam reforming, reforming apparatus provided with structured catalyst for steam reforming, and method for manufacturing structured catalyst for steam reforming
CN118954980A (zh) * 2024-08-23 2024-11-15 北京化工大学 一种双金属碳酸盐白云石加氢炼制的方法
CN119318985A (zh) * 2023-07-15 2025-01-17 中国石油化工股份有限公司 一种生物质转化催化剂及其制备方法和应用
CN120250011A (zh) * 2025-04-01 2025-07-04 河北北方学院 一种纳米增强型生物质制氢膜电极一体化装置及制备方法
CN121534696A (zh) * 2025-12-09 2026-02-17 安徽迪诺环保新材料科技有限公司 汽车尾气降解用镧-铈共掺杂复合二氧化钛制备方法
CN121607162A (zh) * 2026-01-30 2026-03-06 中南大学 碱改性双金属复合催化剂及其制备方法、应用

Families Citing this family (66)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106854037B (zh) * 2016-12-30 2018-03-16 东旭集团有限公司 一种硅酸盐制品及其强化方法
CN108568313B (zh) * 2017-03-07 2020-12-22 中国科学院大连化学物理研究所 一种催化剂及一氧化碳加氢直接转化制低碳烯烃的方法
CN108940355B (zh) * 2017-05-26 2020-12-29 中国科学院大连化学物理研究所 一种碱修饰的催化剂及一氧化碳加氢反应制乙烯的方法
CN108970635B (zh) 2017-06-02 2021-01-19 中国科学院大连化学物理研究所 一种催化剂和合成气直接转化制液体燃料联产低碳烯烃的方法
CN107456927B (zh) * 2017-07-13 2020-06-30 深圳市科力恩生物医疗有限公司 一种基于荧光介孔二氧化硅纳米棒的三维多级孔凝胶及其制备方法
CN109651036B (zh) * 2017-10-10 2022-03-11 中国石油化工股份有限公司 一种由合成气制备低碳烯烃的方法
US11548835B2 (en) 2017-10-30 2023-01-10 Dow Global Technologies Hybrid catalyst for selective and stable olefin production
CN107638888B (zh) * 2017-10-31 2020-08-25 台州路豹鞋业有限公司 一种生产甲乙酮所用催化剂及其制备方法
CN109745965B (zh) * 2017-11-08 2021-11-05 中国科学院大连化学物理研究所 一种含CeZr氧化物的催化剂及一氧化碳加氢直接转化制低碳烯烃的方法
CN107803219B (zh) * 2017-11-16 2021-03-02 中国科学院山西煤炭化学研究所 一种由合成气直接制低碳烯烃催化剂及制备方法和应用
CN109939669B (zh) * 2018-01-26 2020-09-04 中国科学院大连化学物理研究所 一种碱修饰的复合催化剂及一氧化碳加氢反应制乙烯的方法
CN110314695A (zh) * 2018-03-28 2019-10-11 中国科学院大连化学物理研究所 一种复合催化剂、其制备方法和乙烯的制备方法
CN110548523B (zh) * 2018-05-31 2022-04-19 国家能源投资集团有限责任公司 多孔氧化锆基固体酸催化剂及其制备方法和应用
CN110614116A (zh) * 2018-06-20 2019-12-27 中国石油化工股份有限公司 非贵金属系低碳烷烃脱氢催化剂及其制备方法以及低碳烷烃脱氢制低碳烯烃的方法
BR112020024003B1 (pt) 2018-06-29 2023-12-12 Dow Global Technologies Llc Catalisador híbrido e processo para preparar olefinas c2 a c3
US11498059B2 (en) 2018-07-30 2022-11-15 Saudi Arabian Oil Company Catalysts that include iron, cobalt, and copper, and methods for making the same
US10913694B2 (en) 2018-07-30 2021-02-09 Saudi Arabian Oil Company Methods for forming ethylbenzene from polystyrene
CN111068762B (zh) * 2018-10-18 2022-04-05 中国石油化工股份有限公司 费托合成生产低碳烯烃的催化剂和其应用
CN111068742B (zh) * 2018-10-18 2023-04-07 中国石油化工股份有限公司 一步法合成低碳烯烃的催化剂和其应用
CN111068740B (zh) * 2018-10-18 2022-04-01 中国石油化工股份有限公司 费托合成生产低碳烯烃的催化剂及其应用
CN111068640B (zh) * 2018-10-18 2024-03-26 中国石油化工股份有限公司 合成气制低碳烯烃催化剂及在合成气制低碳烯烃中的应用
CN111111751B (zh) * 2018-10-30 2022-08-12 中国石油化工股份有限公司 多组分催化剂、制备方法及其用途
RU2699354C1 (ru) * 2018-11-27 2019-09-05 Федеральное государственное бюджетное учреждение науки "Федеральный исследовательский центр "Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук" (ИК СО РАН) Катализатор защитного слоя для переработки тяжелого нефтяного сырья и способ его приготовления
CN111346672B (zh) * 2018-12-21 2023-07-04 中国科学院大连化学物理研究所 一种掺杂杂原子分子筛催化合成气高选择性制低碳烯烃的方法
CN113498360B (zh) * 2018-12-26 2024-06-14 Ptt全球化学公共有限公司 用于从c4-c7碳氢化合物生产轻质烯烃的催化剂
EP3915681A4 (en) 2019-01-25 2022-11-09 China Petroleum & Chemical Corporation SOLID ACID CATALYST, MANUFACTURE THEREOF AND USE THEREOF
CN109772416B (zh) * 2019-03-04 2021-11-19 南京工业大学 一种含氧空位苯酚加氢催化剂及其制备方法
CN109876814A (zh) * 2019-03-29 2019-06-14 南昌航空大学 一种氧缺陷TiO2@ZnFe2O4异质结光催化材料的制备方法
CN111822026B (zh) * 2019-04-18 2022-10-14 国家能源投资集团有限责任公司 熔铁催化剂及其制备方法和应用
CN112108181A (zh) * 2019-06-21 2020-12-22 中国科学院大连化学物理研究所 一种合成气直接转化制低碳烯烃的催化剂及其制备方法
JP2021003681A (ja) * 2019-06-27 2021-01-14 日本製鉄株式会社 炭化水素製造触媒、炭化水素製造触媒の製造方法、及び炭化水素の製造方法
CN112295590B (zh) * 2019-08-02 2022-09-20 万华化学集团股份有限公司 一种复合金属改性的多级孔分子筛催化剂及其制备方法和应用
CN110743611B (zh) * 2019-10-31 2021-01-01 厦门大学 一种纳米复合催化剂及其制备方法和应用
CN110975926B (zh) * 2019-11-28 2023-05-30 上海应用技术大学 二苯甲醇脱氢合成二苯甲酮催化剂的制备方法及应用
CN112973783B (zh) * 2019-12-14 2022-06-03 中国科学院大连化学物理研究所 一种等级孔催化剂及合成气与c4组分制备低液体燃料的方法
CN112973775B (zh) * 2019-12-14 2023-03-21 中国科学院大连化学物理研究所 一种含mcm-22分子筛的催化剂及其在合成气一步法制液体燃料中的应用
CN110918100A (zh) * 2019-12-16 2020-03-27 云南神脉科技有限公司 一种纳米燃油催化剂及其制备方法与纳米燃油催化器
CN114425363B (zh) * 2020-10-14 2023-08-29 中国石油化工股份有限公司 一步法生产低碳烯烃的催化剂及其制备方法和应用
CN114426550B (zh) * 2020-10-15 2024-04-26 中国石油化工股份有限公司 一种二氧化双环戊二烯dcpddo的制备方法
CN114433196B (zh) * 2020-10-20 2023-07-04 中国石油化工股份有限公司 整体式催化剂、制备方法及其在合成气转化反应中的应用
CN114733565B (zh) * 2021-01-07 2024-04-02 国家能源投资集团有限责任公司 复合催化剂及其制备方法和应用、合成气一步法制低碳烯烃的方法
CN113070081B (zh) * 2021-04-01 2022-10-04 联科华技术有限公司 一种用于除甲醛的多孔磷酸锆基单原子催化剂及其制备方法
CN113209985B (zh) * 2021-04-08 2022-04-26 西南化工研究设计院有限公司 一种用于二甲醚中微量烯烃加氢脱除的催化剂及制备方法和应用
JP2022189628A (ja) * 2021-06-11 2022-12-22 Ｅｎｅｏｓ株式会社 触媒組成物
JP7668885B2 (ja) * 2021-07-29 2025-04-25 Ｔｏｙｏ Ｔｉｒｅ株式会社 １，３－ブタジエン用合成触媒及びその製造方法、並びに１，３－ブタジエンの製造方法
US12258272B2 (en) 2021-08-12 2025-03-25 Saudi Arabian Oil Company Dry reforming of methane using a nickel-based bi-metallic catalyst
US11578016B1 (en) 2021-08-12 2023-02-14 Saudi Arabian Oil Company Olefin production via dry reforming and olefin synthesis in a vessel
US11718575B2 (en) 2021-08-12 2023-08-08 Saudi Arabian Oil Company Methanol production via dry reforming and methanol synthesis in a vessel
US11787759B2 (en) 2021-08-12 2023-10-17 Saudi Arabian Oil Company Dimethyl ether production via dry reforming and dimethyl ether synthesis in a vessel
CN115814786B (zh) * 2021-09-17 2024-06-25 光大环境修复(江苏)有限公司 一种抗氯中毒的脱CVOCs催化剂及其制备方法
CN115999622B (zh) * 2021-10-22 2024-07-23 中国石油化工股份有限公司 一种硅铝型分子筛催化剂及其制备和应用
CN114029072B (zh) * 2021-12-01 2023-07-11 万华化学集团股份有限公司 一种固体超强酸催化剂及用其制备对甲氧基肉桂酸异辛酯的方法
CN114308064B (zh) * 2021-12-22 2023-08-11 东北电力大学 多级孔固体材料限域金属基催化剂及其制备方法和应用
US11617981B1 (en) 2022-01-03 2023-04-04 Saudi Arabian Oil Company Method for capturing CO2 with assisted vapor compression
CN114289042B (zh) * 2022-01-10 2023-05-30 万华化学集团股份有限公司 一种介孔固体酸催化剂、制备方法及其应用
CN114570417B (zh) * 2022-03-23 2023-06-27 清华大学 用于正丁醇制丁烯的催化剂及其制备方法和制备丁烯的方法
CN115282988B (zh) * 2022-10-08 2023-01-13 浙江晟格生物科技有限公司 一种应用于制备生物糖的固体酸催化剂及制备方法
CN115924936B (zh) * 2022-12-09 2025-05-23 万华化学集团股份有限公司 一种甲酰胺脱水制氢氰酸的方法
CN116344878B (zh) * 2023-03-22 2026-05-26 中国科学院大连化学物理研究所 一种燃料电池用复合型高温质子交换膜及其制备方法和应用
CN119303588B (zh) * 2023-07-13 2026-02-06 中国石油天然气股份有限公司 一种多级孔钼铋复合金属氧化物催化剂及其制备方法与应用
KR102954789B1 (ko) * 2023-09-22 2026-04-21 지에스칼텍스 주식회사 석유대체유기물 생산을 위한 이산화탄소 전환용 촉매 및 이의 제조방법
CN119951556B (zh) * 2023-11-09 2025-11-25 中国石油化工股份有限公司 一种铁基介孔分子筛催化剂及其制备方法和应用
WO2025110685A1 (ko) * 2023-11-20 2025-05-30 지에스칼텍스 주식회사 제올라이트를 활용하여 액상연료 수율이 향상된 이산화탄소 전환용 촉매 시스템
CN118744011B (zh) * 2024-06-24 2025-04-11 青岛科技大学 一种金属负载型复合分子筛催化剂及其制备方法和应用
CN119657163A (zh) * 2024-12-02 2025-03-21 常州大学 一种用于co加氢催化合成轻质烯烃的高熵催化剂及其制备方法和应用
CN120774982B (zh) * 2025-09-08 2025-11-25 湖南人文科技学院 一种新橙皮苷一步合成新橙皮苷二氢查尔酮的方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102219629A (zh) * 2010-04-15 2011-10-19 中国石油化工股份有限公司 甲醇转化制低碳烯烃的方法
US20120219735A1 (en) * 2011-02-27 2012-08-30 The Board Of Trustees Of The University Of Alabama Methods for preparing and using metal and/or metal oxide porous materials
US20140107371A1 (en) * 2012-10-16 2014-04-17 Board Of Trustees Of The University Of Alabama Catalysis by metal nanoparticles dispersed within a hierarchically porous carbon material
CN104056627A (zh) * 2013-03-21 2014-09-24 中国科学院大连化学物理研究所 一种合成气制低碳烯烃催化剂及其在费托反应中的应用
CN104307560A (zh) * 2014-10-20 2015-01-28 丁泳 以甲醇为原料制备丙烯副产高辛烷值汽油的催化剂及其制备方法

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2571274A1 (fr) 1984-10-04 1986-04-11 Centre Nat Rech Scient Catalyseurs metal de transition-manganese sur supports, leur preparation et leur utilisation dans un procede de transformation selective du gaz de synthese en olefines legeres
CN1036131C (zh) * 1991-06-22 1997-10-15 中国科学院大连化学物理研究所 一种由合成气直接制取低碳烯烃方法
CN1040397C (zh) 1992-09-03 1998-10-28 中国科学院大连化学物理研究所 合成气制低碳烯烃含铁锰催化剂及合成反应
EP1063013B1 (en) 1999-06-24 2005-10-12 ENI S.p.A. Catalytic composition for the aromatization of hydrocarbons
JP4750303B2 (ja) 2001-03-23 2011-08-17 水澤化学工業株式会社 メソポーラスシリカアルミナゲル、調湿剤及び触媒担体
EP1396481A1 (en) 2002-08-14 2004-03-10 ATOFINA Research Production of olefins
JP2006512274A (ja) 2002-12-31 2006-04-13 コーニング インコーポレイテッド ＺｎＯベースのガラスセラミック
JP2007181755A (ja) * 2006-01-05 2007-07-19 Nippon Gas Gosei Kk 液化石油ガス製造用触媒、および、この触媒を用いた液化石油ガスの製造方法
FR2920758B1 (fr) * 2007-09-07 2009-11-13 Inst Francais Du Petrole Materiau cristallise a porosite hierarchisee et comprenant du silicium
CN101396662A (zh) 2007-09-28 2009-04-01 北京化工大学 一种用于合成气制低碳烯烃的纳米催化剂及制备方法
CN101745403B (zh) 2008-12-18 2012-09-12 中国石油化工股份有限公司 一种由合成气制备甲醇、二甲醚和低碳烯烃的方法
CN102369261B (zh) * 2009-03-30 2014-12-17 一般财团法人石油能源技术中心 烷基苯的生产方法及其使用的催化剂
SG181865A1 (en) * 2009-12-22 2012-08-30 Nippon Catalytic Chem Ind Catalyst for treatment of waste water, and method for treatment of waste water using the catalyst
RU2524217C2 (ru) 2012-08-07 2014-07-27 ИНФРА ИксТиЭл ТЕКНОЛОДЖИ ЛИМИТЕД Катализатор для прямого получения синтетической нефти, обогащенной изопарафинами, и способ его получения
CN103100415B (zh) * 2012-12-03 2015-06-10 北京化工大学 活性组分纳米颗粒嵌入分子筛结晶的催化剂、方法及应用
CN103979570B (zh) 2014-05-14 2016-01-06 武汉理工大学 一种新型有序大孔-介孔-微孔多级孔硅铝分子筛的合成方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102219629A (zh) * 2010-04-15 2011-10-19 中国石油化工股份有限公司 甲醇转化制低碳烯烃的方法
US20120219735A1 (en) * 2011-02-27 2012-08-30 The Board Of Trustees Of The University Of Alabama Methods for preparing and using metal and/or metal oxide porous materials
US20140107371A1 (en) * 2012-10-16 2014-04-17 Board Of Trustees Of The University Of Alabama Catalysis by metal nanoparticles dispersed within a hierarchically porous carbon material
CN104056627A (zh) * 2013-03-21 2014-09-24 中国科学院大连化学物理研究所 一种合成气制低碳烯烃催化剂及其在费托反应中的应用
CN104307560A (zh) * 2014-10-20 2015-01-28 丁泳 以甲醇为原料制备丙烯副产高辛烷值汽油的催化剂及其制备方法

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3318327A4 *

Cited By (69)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3593901A4 (en) * 2016-12-30 2020-11-04 Shanghai Advanced Research Institute, Chinese Academy of Sciences CATALYST FOR THE PREPARATION OF HYDROCARBONS FROM CARBON DIOXIDE BY ONE-STEP HYDROGENATION AND ITS PREPARATION PROCESS
CN106984303B (zh) * 2017-04-28 2019-09-10 武汉理工大学 一种担载贵金属的等级孔大孔-介孔γ-Al2O3催化剂及其制备方法
CN106984303A (zh) * 2017-04-28 2017-07-28 武汉理工大学 一种担载贵金属的等级孔大孔‑介孔γ‑Al2O3催化剂及其制备方法
CN110691646A (zh) * 2017-05-31 2020-01-14 古河电气工业株式会社 Co变换或逆变换催化剂结构体及其制造方法、co变换或逆变换反应装置、二氧化碳和氢的制造方法、以及一氧化碳和水的制造方法
US11648543B2 (en) 2017-05-31 2023-05-16 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US12030041B2 (en) 2017-05-31 2024-07-09 Furukawa Electric Co., Ltd. Structured catalyst for steam reforming, reforming apparatus provided with structured catalyst for steam reforming, and method for manufacturing structured catalyst for steam reforming
WO2018221706A1 (ja) * 2017-05-31 2018-12-06 古河電気工業株式会社 メタノール改質触媒構造体、メタノール改質用装置、メタノール改質触媒構造体の製造方法及びオレフィンまたは芳香族炭化水素の少なくとも一方の製造方法
US11547987B2 (en) 2017-05-31 2023-01-10 Furukawa Electric Co., Ltd. Structured catalyst for oxidation for exhaust gas purification, method for producing same, automobile exhaust gas treatment device, catalytic molding, and gas purification method
JP7269169B2 (ja) 2017-05-31 2023-05-08 古河電気工業株式会社 メタノール改質触媒構造体、メタノール改質用装置、メタノール改質触媒構造体の製造方法及びオレフィンまたは芳香族炭化水素の少なくとも一方の製造方法
US11648538B2 (en) 2017-05-31 2023-05-16 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US12115523B2 (en) 2017-05-31 2024-10-15 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US11648542B2 (en) 2017-05-31 2023-05-16 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
US11904306B2 (en) 2017-05-31 2024-02-20 Furukawa Electric Co., Ltd. Catalyst structure and method for producing the catalyst structure
US11684909B2 (en) 2017-05-31 2023-06-27 Furukawa Electric Co., Ltd. Structured catalyst for methanol reforming, methanol reforming device, method for producing structured catalyst for methanol reforming, and method for producing at least one of olefin or aromatic hydrocarbon
US11161101B2 (en) 2017-05-31 2021-11-02 Furukawa Electric Co., Ltd. Catalyst structure and method for producing the catalyst structure
JPWO2018221706A1 (ja) * 2017-05-31 2020-03-26 古河電気工業株式会社 メタノール改質触媒構造体、メタノール改質用装置、メタノール改質触媒構造体の製造方法及びオレフィンまたは芳香族炭化水素の少なくとも一方の製造方法
US11680211B2 (en) 2017-05-31 2023-06-20 Furukawa Electric Co., Ltd. Structured catalyst for hydrodesulfurization, hydrodesulfurization device including the structured catalyst, and method for producing structured catalyst for hydrodesulfurization
US11666894B2 (en) 2017-05-31 2023-06-06 Furukawa Electric Co., Ltd. Structured catalyst for CO shift or reverse shift and method for producing same, CO shift or reverse shift reactor, method for producing carbon dioxide and hydrogen, and method for producing carbon monoxide and water
US11654422B2 (en) 2017-05-31 2023-05-23 Furukawa Electric Co., Ltd. Structured catalyst for catalytic cracking or hydrodesulfurization, catalytic cracking apparatus and hydrodesulfurization apparatus including the structured catalyst, and method for producing structured catalyst for catalytic cracking or hydrodesulfurization
US11655157B2 (en) 2017-05-31 2023-05-23 National University Corporation Hokkaido University Functional structural body and method for making functional structural body
EP3632557A4 (en) * 2017-06-02 2021-01-20 Dalian Institute Of Chemical Physics Chinese Academy of Sciences CATALYST AND METHOD FOR DIRECT CONVERSION OF SYNTHESIS GAS FOR THE PRODUCTION OF LIGHT OLEFINS
CN109304220A (zh) * 2017-07-28 2019-02-05 中国石油化工股份有限公司 合成气制备低碳烯烃的催化剂
WO2019030279A1 (en) * 2017-08-08 2019-02-14 Basf Se COMPOSITION COMPRISING A MIXED METAL OXIDE AND A MOLDING COMPRISING A ZEOLITHIC MATERIAL HAVING A TYPE OF CHA STRUCTURE AND AN ALKALINE-EARTH METAL
JP2019038777A (ja) * 2017-08-25 2019-03-14 国立大学法人富山大学 低級オレフィンの製造方法
CN109651030A (zh) * 2017-10-10 2019-04-19 中国石油化工股份有限公司 合成气直接制备低碳烯烃的方法
CN109701596A (zh) * 2017-10-26 2019-05-03 中国石油化工股份有限公司 催化剂体系
CN109701601A (zh) * 2017-10-26 2019-05-03 中国石油化工股份有限公司 组合催化剂体系及其用途
CN109847791A (zh) * 2017-11-30 2019-06-07 中国科学院大连化学物理研究所 一种催化剂、其制备方法及在丁烯歧化反应中的应用
EP3744423A4 (en) * 2018-01-26 2021-11-03 Dalian Institute of Chemical Physics, Chinese Academy of Sciences CATALYST AND METHOD FOR THE DIRECT CONVERSION OF SYNTHESIS GAS INTO A LOW CARBON OLEFIN
JP2021516146A (ja) * 2018-01-26 2021-07-01 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ 触媒及び合成ガスの直接転化による低級オレフィンの製造方法
EP3744426A4 (en) * 2018-01-26 2021-11-03 Dalian Institute of Chemical Physics, Chinese Academy of Sciences CATALYST WITH LF TYPE B ACID AND PROCESS FOR THE DIRECT CONVERSION OF SYNTHESIS GAS INTO ETHYLENE
EP3744424A4 (en) * 2018-01-26 2021-11-03 Dalian Institute of Chemical Physics, Chinese Academy of Sciences COMPOSITE CATALYST MODIFIED WITH ORGANIC BASE AND PROCESS FOR PRODUCING ETHYLENE BY HYDROGENATION OF CARBON MONOXIDE
EP3744425A4 (en) * 2018-01-26 2021-11-03 Dalian Institute of Chemical Physics, Chinese Academy of Sciences SUPPORTED CATALYST AND METHOD FOR DIRECT CONVERSION OF SYNTHESIS GAS TO LOW CARBON OLEFINE
JP7007763B2 (ja) 2018-01-26 2022-02-10 中国科学院大▲連▼化学物理研究所 有機アルカリで修飾された複合触媒及び一酸化炭素の水素化によるエチレンの製造方法
JP7007762B2 (ja) 2018-01-26 2022-02-10 中国科学院大▲連▼化学物理研究所 触媒及び合成ガスの直接転化による低級オレフィンの製造方法
JP2021516147A (ja) * 2018-01-26 2021-07-01 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ 有機アルカリで修飾された複合触媒及び一酸化炭素の水素化によるエチレンの製造方法
US20210268482A1 (en) * 2018-06-29 2021-09-02 Dow Global Technologies Llc Hybrid catalysts comprising a zeolite and a mixed metal oxide component for converting syngas into c2 and c3 olefins
US11884605B2 (en) * 2018-06-29 2024-01-30 Dow Global Technologies Llc Hybrid catalysts comprising a zeolite and a mixed metal oxide component for converting syngas into C2 and C3 olefins
CN109331863A (zh) * 2018-07-02 2019-02-15 山东科技大学 一种原位掺碳型镍基介孔催化剂的制备和应用
CN109289865A (zh) * 2018-09-30 2019-02-01 中国科学院山西煤炭化学研究所 一种合成气制低碳混合醇的含硅催化剂及制法和应用
CN111111760B (zh) * 2018-10-30 2022-10-11 中国石油化工股份有限公司 二氧化碳加氢制取低碳烯烃的催化剂及其用途
CN111111760A (zh) * 2018-10-30 2020-05-08 中国石油化工股份有限公司 二氧化碳加氢制取低碳烯烃的催化剂及其用途
CN111111764A (zh) * 2018-10-30 2020-05-08 中国石油化工股份有限公司 催化剂体系及其用途
CN112108180A (zh) * 2019-06-21 2020-12-22 中国科学院大连化学物理研究所 一种合成气直接转化制低碳烯烃的催化剂及其制备方法
CN110474060A (zh) * 2019-07-01 2019-11-19 吉林大学 一种高效三维网状氮自掺杂碳气凝胶的制备方法及氧还原催化剂应用
CN110474060B (zh) * 2019-07-01 2022-08-30 吉林大学 一种高效三维网状氮自掺杂碳气凝胶的制备方法及氧还原催化剂应用
CN110229380A (zh) * 2019-07-08 2019-09-13 福建远翔新材料股份有限公司 一种高效、高透明二氧化硅塑料薄膜开口剂的制备方法
CN112705218B (zh) * 2019-10-24 2023-11-28 中国石油化工股份有限公司 合成气制低碳烯烃的催化剂、制备方法及其应用
CN112705218A (zh) * 2019-10-24 2021-04-27 中国石油化工股份有限公司 合成气制低碳烯烃的催化剂、制备方法及其应用
CN111195521A (zh) * 2020-01-15 2020-05-26 大连凯信科技研发有限公司 烯烃催化剂及其制备方法以及在合成气制烯烃中的应用
CN111195521B (zh) * 2020-01-15 2023-01-17 大连凯信科技研发有限公司 烯烃催化剂及其制备方法以及在合成气制烯烃中的应用
CN113385191B (zh) * 2020-03-13 2022-11-18 湘潭大学 无机固体硅基磺酸和/或磷酸催化剂及其制备方法和应用
CN113385191A (zh) * 2020-03-13 2021-09-14 湘潭大学 无机固体硅基磺酸和/或磷酸催化剂及其制备方法和应用
CN111519073A (zh) * 2020-06-03 2020-08-11 上海鑫烯复合材料工程技术中心有限公司 一种具有三峰特征的纳米增强金属基复合材料
CN111519073B (zh) * 2020-06-03 2021-07-09 上海鑫烯复合材料工程技术中心有限公司 一种具有三峰特征的纳米碳增强金属基复合材料
CN111644169B (zh) * 2020-06-17 2023-02-28 宁夏大学 金属复合改性纳米氧化锆催化剂及其制备方法和应用
CN111644169A (zh) * 2020-06-17 2020-09-11 宁夏大学 金属复合改性纳米氧化锆催化剂及其制备方法和应用
CN113600214A (zh) * 2021-09-02 2021-11-05 广州大学 一种核壳型Fe2O3@TixOy-Pz光催化剂的制备方法及应用
CN113600214B (zh) * 2021-09-02 2023-10-24 广州大学 一种核壳型Fe2O3@TixOy-Pz光催化剂的制备方法及应用
CN116020435A (zh) * 2021-10-27 2023-04-28 中国石油化工股份有限公司 贵金属负载铟锆碳复合材料及其制备方法和二氧化碳加氢制备甲醇的方法
CN116060113A (zh) * 2021-10-29 2023-05-05 中国石油化工股份有限公司 一种直馏柴油加氢改质催化剂及其制备方法和应用
CN116060113B (zh) * 2021-10-29 2024-05-07 中国石油化工股份有限公司 一种直馏柴油加氢改质催化剂及其制备方法和应用
CN116285128A (zh) * 2023-04-23 2023-06-23 罗孚橡胶（江苏）有限公司 一种高强度耐老化橡胶及其制备方法
CN116285128B (zh) * 2023-04-23 2024-01-12 罗孚橡胶（江苏）有限公司 一种高强度耐老化橡胶及其制备方法
CN119318985A (zh) * 2023-07-15 2025-01-17 中国石油化工股份有限公司 一种生物质转化催化剂及其制备方法和应用
CN118954980A (zh) * 2024-08-23 2024-11-15 北京化工大学 一种双金属碳酸盐白云石加氢炼制的方法
CN120250011A (zh) * 2025-04-01 2025-07-04 河北北方学院 一种纳米增强型生物质制氢膜电极一体化装置及制备方法
CN121534696A (zh) * 2025-12-09 2026-02-17 安徽迪诺环保新材料科技有限公司 汽车尾气降解用镧-铈共掺杂复合二氧化钛制备方法
CN121607162A (zh) * 2026-01-30 2026-03-06 中南大学 碱改性双金属复合催化剂及其制备方法、应用

Also Published As

Publication number Publication date
EP3318327A1 (en) 2018-05-09
ZA201708553B (en) 2018-12-19
JP2018520862A (ja) 2018-08-02
CN106311317B (zh) 2019-04-16
RU2706241C2 (ru) 2019-11-15
JP6666365B2 (ja) 2020-03-13
US10532961B2 (en) 2020-01-14
SA517390644B1 (ar) 2021-07-07
RU2018103755A3 (zh) 2019-08-05
RU2018103755A (ru) 2019-08-05
US20180194700A1 (en) 2018-07-12
CN106311317A (zh) 2017-01-11
EP3318327A4 (en) 2019-02-27

Similar Documents

Publication Publication Date Title
JP6666365B2 (ja) 一段階法によって合成ガスから軽質オレフィンを直接調製する触媒及び方法
CN109939728B (zh) 一种负载催化剂及合成气直接转化制低碳烯烃的方法
CN111346672B (zh) 一种掺杂杂原子分子筛催化合成气高选择性制低碳烯烃的方法
Masudi et al. Opportunities for less-explored zeolitic materials in the syngas-to-olefins pathway over nanoarchitectured catalysts: a mini review
WO2020125487A1 (zh) 一种掺杂杂原子分子筛催化合成气高选择性制低碳烯烃的方法
CN108940355B (zh) 一种碱修饰的催化剂及一氧化碳加氢反应制乙烯的方法
TW200942326A (en) Catalytic composition for producing olefins by catalytic cracking
CN114054077A (zh) 核壳型复合催化剂及其制备方法和用途
CN109663613B (zh) 一种金属改性zsm-5分子筛催化剂及其制备和应用
CN104525245A (zh) 一种纳米晶堆积介微孔zsm-5催化剂及制备和应用
CN107774302B (zh) 一种催化剂及合成气直接转化制液体燃料联产低碳烯烃的方法
EP3558869B1 (en) Process to convert synthesis gas to olefins using a bifunctional chromium / zinc oxide-sapo-34 catalyst
CN108970638A (zh) 一种催化剂与合成气直接转化制液体燃料联产低碳烯烃的方法
CN110560153A (zh) 一种铝共享金属-沸石双功能催化剂及制备方法和应用
CN111346666B (zh) 一种催化剂及合成气直接转化制高芳烃含量的液体燃料的方法
WO2018219364A1 (zh) 一种催化剂及合成气直接转化制液体燃料联产低碳烯烃的方法
WO2020253712A1 (zh) 一种合成气直接转化制低碳烯烃的催化剂及其制备方法
CN107661773B (zh) 一种催化剂及合成气直接转化制液体燃料联产低碳烯烃的方法
CA2983738A1 (en) Method of manufacturing iron-based catalysts and method of manufacturing hydrocarbons using iron-based catalysts made by the method
CN112295597B (zh) 一种催化合成气直接转化制富含btx的芳烃的催化剂及其应用
US20100249252A1 (en) Zr-fe catalysts for fischer-tropsch synthesis
Chen et al. In situ incorporation of W into hierarchical ZSM–5 zeolites for efficient production of propylene in 1-hexene catalytic cracking
CN101768040A (zh) 用于丁烯和乙烯制丙烯的方法
CN111346669A (zh) 一种掺杂杂原子分子筛催化合成气高选择性制低碳烯烃的方法
CN116351462B (zh) 一种甲醇制丙烯催化剂及其制备方法

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: 15896956

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2017567812

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 2018103755

Country of ref document: RU

WWW Wipo information: withdrawn in national office

Ref document number: 2015896956

Country of ref document: EP