WO2015007230A1 - 一种铁基加氢催化剂及其应用 - Google Patents

一种铁基加氢催化剂及其应用 Download PDF

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Publication number
WO2015007230A1
WO2015007230A1 PCT/CN2014/082463 CN2014082463W WO2015007230A1 WO 2015007230 A1 WO2015007230 A1 WO 2015007230A1 CN 2014082463 W CN2014082463 W CN 2014082463W WO 2015007230 A1 WO2015007230 A1 WO 2015007230A1
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Prior art keywords
active component
iron
hydrogenation catalyst
based hydrogenation
component metal
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PCT/CN2014/082463
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English (en)
French (fr)
Inventor
申宝剑
李�浩
王艳丹
李建聪
李磊
申波俊
申宝华
王闻年
袁德林
许红亮
Original Assignee
中国石油大学(北京)
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Priority claimed from CN201310303258.4A external-priority patent/CN104383923B/zh
Priority claimed from CN201310302954.3A external-priority patent/CN104383922B/zh
Application filed by 中国石油大学(北京) filed Critical 中国石油大学(北京)
Priority to CA2917361A priority Critical patent/CA2917361C/en
Priority to US14/905,719 priority patent/US10335773B2/en
Priority to CN201480000780.8A priority patent/CN104918698B/zh
Priority to EP14826159.7A priority patent/EP3023147B1/en
Publication of WO2015007230A1 publication Critical patent/WO2015007230A1/zh

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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/80Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14Phosphorus; Compounds thereof
    • B01J27/185Phosphorus; Compounds thereof with iron group metals or platinum group metals
    • B01J27/1853Phosphorus; Compounds thereof with iron group metals or platinum group metals with iron, cobalt or nickel
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14Phosphorus; Compounds thereof
    • B01J27/186Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/195Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with vanadium, niobium or tantalum
    • B01J27/198Vanadium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/60Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61Surface area
    • B01J35/61310-100 m2/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/60Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61Surface area
    • B01J35/615100-500 m2/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/60Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63Pore volume
    • B01J35/633Pore volume less than 0.5 ml/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/60Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63Pore volume
    • B01J35/6350.5-1.0 ml/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/60Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64Pore diameter
    • B01J35/6472-50 nm
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02Impregnation, coating or precipitation
    • B01J37/03Precipitation; Co-precipitation
    • B01J37/031Precipitation
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08Heat treatment
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/20Sulfiding
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44Hydrogenation of the aromatic hydrocarbons
    • C10G45/46Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00Constitutive chemical elements of heterogeneous catalysts

Definitions

  • the invention relates to an iron-based hydrogenation catalyst and application thereof, and belongs to the technical field of hydrogenation catalysts in the field of petroleum refining.
  • CN101439289A discloses a method for in-situ reaction in a pore of a carrier to form a nickel molybdate (cobalt) or nickel tungstate (cobalt) compound by using urea or ammonia as a reaction aid, thereby avoiding metal and
  • the reaction of the carrier makes the active component more susceptible to vulcanization, increasing the activity of the hydrogenation catalyst.
  • the carrier in the conventional supported catalyst including the above-mentioned prior art hydrogenation catalyst has no activity or activity, and the proportion of the carrier is large, the catalytic activity of the supported catalyst is difficult to satisfy the production of ultra-low sulfur diesel. Requirements. Therefore, in recent years, an unsupported carrier which is indispensable in the conventional hydrogenation catalyst, and a non-supported (Bulk) catalyst mainly composed of an oxide or a sulfide of nickel, cobalt, tungsten, molybdenum having a pore structure itself as a main component has appeared. .
  • US 6,582,590 discloses a process for the preparation of unsupported hydrogenation catalysts by direct precipitation by dissolving soluble molybdates and tungstates in water, mixing with lye, and dissolving the soluble nickel salts in water at 90°. It is kept under C, and then an alkali solution of molybdenum and tungstate is added at a certain speed, and finally, an unsupported hydrodesulfurization catalyst is obtained by filtration and drying.
  • a method for preparing a similar unsupported hydrogenation catalyst is also disclosed in US Pat. No. 6,712,955, US Pat. No. 6,156, 695, and US Pat. No. 6,678, 663, all of which are incorporated herein by reference. metal.
  • CN101255356A also discloses a preparation method of preparing a nickel (cobalt)-tungsten (molybdenum) non-supporting catalyst having a nanopore and a high specific surface area by a urea melt reaction, and the catalyst prepared by the method has a good addition. Hydrogen treatment activity.
  • CN1086534A discloses a heavy oil hydrodenitrogenation catalyst and a preparation method thereof.
  • the composition of the catalyst is W-Mo-Ni/Si0 2 -B 2 0 3 -Al 2 0 3 .
  • CN1458236A discloses a heavy oil hydrodemetallization and desulfurization catalyst, the active component of which comprises 1% by weight to 20% by weight of tungsten oxide and/or molybdenum oxide, 0.5% by weight to 5.0% by weight of nickel oxide and/or cobalt oxide.
  • the adjuvant contains from 0.1% by weight to 3.0% by weight of an alkali metal and/or alkaline earth metal oxide.
  • the catalyst prepared by the method has high demetallization activity and desulfurization activity at the same time, and has high activity stability, especially stability of desulfurization activity.
  • CN1110304A discloses a heavy oil hydrotreating catalyst which supports molybdenum, nickel and phosphorus with alumina containing silicon and phosphorus as a carrier.
  • the catalyst contained 10-30 wt% MoO 3 , 2-6 wt% NiO, 2-6 wt% P, which exhibited good denitrification performance.
  • USP727980 discloses a hydrodemetallization catalyst and a preparation method thereof, which is based on a sintered oxide (A1 2 0 3 , Si0 2 , Ti0 2 or a mixture thereof), first impregnating ferric nitrate, and then passing through After drying and calcination, the ammonium molybdate solution is further immersed, and then dried and melted to obtain a finished catalyst having two crystal phases.
  • the catalyst has high metal content and high hydrogenation activity, but the catalyst has the disadvantages of complicated preparation process and high price.
  • CN102039140A discloses a heavy oil hydrotreating catalyst and a preparation method thereof, which mainly use inexpensive natural clays such as kaolin, montmorillonite, diatomaceous earth and natural clay as part of a carrier.
  • CN1289821A discloses a high activity residue hydroconversion catalyst and a preparation method thereof.
  • the catalyst is prepared by using a completely kneading method, using titanium as an auxiliary agent, mixing the aluminum hydroxide dry rubber powder and the molecular sieve in a certain ratio, and then adding an alkaline solution of the VIB metal first, and then adding the VIII group and/or the VIB group. An acidic solution of metal.
  • the catalyst had a pore volume of 0.36-0.60 mL/g and a specific surface area of 190-280 m 2 /g. Since the method adopts a simple and convenient kneading preparation method, the cost is lower than that of the dipping method and the precipitation method.
  • an object of the present invention is to provide an iron-based hydrogenation catalyst suitable for use in gasoline, diesel oil, heavy oil, and the like, and use thereof.
  • the iron-based hydrogenation catalyst of the invention has iron as the main active component metal and zinc and potassium as the first auxiliary active component metal, and has the advantages of low production cost and simple manufacturing process.
  • the present invention provides an iron-based hydrogenation catalyst, wherein the iron-based hydrogenation catalyst uses iron as a main active component metal, and zinc and potassium as a first auxiliary component metal (also referred to as a first auxiliary active component element); the total amount of the main active component metal and the auxiliary active component element is from 5 to 100% based on the total weight of the iron-based hydrogenation catalyst, and the balance is a bond Or a carrier, in the form of an oxide; the co-active component element comprises a first co-active component metal;
  • the molar ratio of the main active component metal to the first co-active component metal is from 0.5 to 200: 1 (preferably from 0.8 to 20: 1).
  • the iron-based hydrogenation catalyst further comprises a second auxiliary active component element selected from the group consisting of IVB, VA, VB, VIB and Group VIII elements, wherein the IVB element is preferably titanium or zirconium.
  • the VA element is preferably phosphorus
  • the VB element is preferably vanadium
  • the VIB element is preferably chromium
  • the VIII element is preferably cobalt, nickel, palladium and platinum; the molar ratio of the main active component metal to the second coactive component element is 0.5.
  • the co-active component element comprises a first co-active component metal and a second co-active component element.
  • the determination and calculation of the total content of the main active component metal and the co-active component element (metal) in the catalyst can be carried out in the form of oxides by measurement and calculation methods well known in the art.
  • the above iron-based hydrogenation catalyst provided by the present invention may be composed only of a main active component metal, a co-active component element (may be a single first active component metal, or a first auxiliary component metal and a second a combination of a co-active component element, without a binder and a carrier, that is, a total amount of the main active component metal and the co-active component element is 100%, and the iron-based hydrogenation catalyst of this composition may It is prepared by a tablet molding method, that is, a main active component metal and a co-active component are mixed and directly tablet-formed.
  • the iron-based hydrogenation catalyst may also be composed of a main active component metal, a co-active component element, a binder or a carrier, and an iron-based hydrogenation catalyst using a binder may be prepared by a coprecipitation method.
  • Carrier iron base The hydrogenation catalyst can be prepared by an impregnation method.
  • the total amount of the main active component metal and the co-active component element is from 20 to 70% based on the total weight of the iron-based hydrogenation catalyst (more preferably 20-50%), the balance being a binder or a carrier, in the form of an oxide, the auxiliary active component element comprising the first co-active component metal or the first co-active component metal and the second co-active group A combination of sub-elements.
  • the above iron-based hydrogenation catalyst is prepared by a dipping method, a coprecipitation method or a tablet molding method.
  • the impregnation method comprises the steps of:
  • the catalyst semi-finished product is allowed to stand in the air for 2 to 24 hours, then dried, and then calcined in an air atmosphere at 200 to 800 ° C for 2 to 8 hours to obtain an iron-based hydrogenation catalyst.
  • the iron-based hydrogenation catalyst contains the second co-active component element, the salt of the second co-active component element and the salt of the main active component metal, the first co-active component
  • the metal salts are dissolved together in deionized water.
  • the volume of the immersion liquid is the same as the saturated water absorption amount of the carrier.
  • the drying of the catalyst semi-finished product is carried out in an oven at 120 °C.
  • the catalyst semi-finished product is heated at a rate of 5 ° C/min when calcined.
  • the carrier used comprises pyrite (FeS 2 ), pyrrhotite (F ei _ x S), ferric oxide, triiron tetroxide, alumina, two A combination of one or more of silicon oxide, amorphous silicon aluminum, and zeolite molecular sieves, and the like.
  • the coprecipitation method comprises the steps of:
  • reaction is stirred in a 40-95 Torr water bath for l-24 h, and then allowed to stand in a 40-95 ° C water bath for aging for 2-48 h to obtain a precipitate;
  • the catalyst precursor is calcined in an air atmosphere at 200-800 ° C for 2-8 h to obtain a metal oxide
  • the metal oxide is mixed with a binder to carry out a molding treatment to obtain an iron-based hydrogenation catalyst.
  • the iron-based hydrogenation catalyst contains the second auxiliary active component element, the salt of the second auxiliary active component element and the salt of the main active component metal, the first aid Salt of active component metal together with sink The aqueous solution of the precipitant is mixed.
  • the molding treatment may be extrusion molding or kneading molding.
  • the conventionally used phthalocyanine powder or the like may be used as a squeezing agent, citric acid, acetic acid, nitric acid or the like as a peptizing agent, mixed with a metal oxide and a binder, and then subjected to a molding operation such as extrusion or kneading. .
  • the coprecipitation method further comprises the steps of: further calcining the iron-based hydrogenation catalyst obtained after the molding treatment; more preferably, the calcination condition is: 5° The heating rate of C/min was raised and calcined in an air atmosphere at 200-800 ° C for 2-8 h.
  • the binder used in the iron-based hydrogenation catalyst of the present invention comprises one or a combination of alumina, silica sol, aluminum sol, water glass and the like.
  • the amount of the binder can be determined according to the composition of the iron-based hydrogenation catalyst, and can be generally controlled to be 10% to 95% by weight based on the total weight of the iron-based hydrogenation catalyst.
  • the precipitate is filtered, washed with water, and dried, it may be pulverized as appropriate, and then the obtained catalyst precursor is calcined.
  • the drying of the precipitate is carried out in an oven at 120 °C.
  • the catalyst precursor is heated at a rate of 5 ° C/min when calcined.
  • the precipitating agent includes one of NaOH, KOH, Na 2 C0 3 , K 2 C0 3 , Na 2 S, (NH 4 ) 2 S, urea, and ammonia water or the like.
  • the molar ratio of the precipitant to the main active component metal, the first co-active component metal, the second co-active component element is 1-6: 1, that is, a precipitant The ratio of the molar amount to the sum of the molar amounts of the three.
  • ammonia water is used as a precipitant, it can be used as it is without the need to prepare an aqueous solution of a precipitant.
  • the concentration of the aqueous solution of the salt of the main active component metal and the salt of the auxiliary active component element and the concentration of the aqueous solution of the precipitating agent can be conventionally regulated by those skilled in the art as long as the above ratio can be satisfied. The relationship can make the reaction go smoothly.
  • the aqueous solution of the salt of the main active component metal and the salt of the auxiliary active component element may be an aqueous solution in which the salt of the main active component metal and the salt of the auxiliary active component element are respectively dissolved in deionized water and mixed.
  • the specific operation of mixing the salt of the main active component metal and the aqueous solution of the salt of the co-active component element and the aqueous solution of the precipitating agent may be a method of adding an aqueous solution of the precipitating agent to the salt of the main active component metal and the auxiliary active component element.
  • the salt is in an aqueous solution and stirred well.
  • the tableting process comprises the steps of:
  • the oxide powder of the iron-based hydrogenation catalyst is subjected to tableting in a tableting machine to obtain an iron-based hydrogenation catalyst.
  • the iron-based hydrogenation catalyst contains the second auxiliary component element, the salt of the second auxiliary component element and the salt of the main active component metal, the first auxiliary active group The metal salts are mixed together.
  • the salt of the main active component metal includes one or more of iron nitrate, iron sulfate, iron chloride, and iron phosphate. combination.
  • the salt of the first co-active component metal includes one or more of a nitrate, a sulfate, a chloride, a phosphate, and the like. Combination of species.
  • the salt of the second auxiliary active component element includes one or more of a nitrate, a sulfate, a chloride salt, and a phosphate salt. Combination of species.
  • the invention also provides the above-mentioned gasoline-diesel and heavy oil iron-based hydrogenation catalysts in the direct-stroke gasoline, the direct-dip diesel, the coking gasoline, the coking diesel, the catalytic cracking gasoline, the catalytic cracking diesel oil, the atmospheric residue, the vacuum residue, the coal tar
  • the hydrotreating may include hydrodesulfurization, hydrodenitrogenation, hydrosaturation of aromatic hydrocarbons, hydrodemetallization, and the like.
  • the iron-based hydrogenation catalyst of the present invention can be obtained by the above-mentioned impregnation method, coprecipitation method or tablet molding method, and can be subjected to a vulcanization treatment to achieve high activity.
  • the vulcanization treatment can be carried out by a vulcanization technique of a hydrogenation catalyst conventional in the art, and the vulcanized oil or vulcanizing agent or the like used can also be a vulcanized oil or a vulcanizing agent conventionally used in the art.
  • the vulcanization treatment temperature may be 200-450 ° C, the pressure may be 0.1-10 MPa, the time may be 2-48 hours, the liquid hourly space velocity may be Ol Oh- 1 , and the hydrogen oil volume ratio may be 100-800; preferably, The vulcanization temperature is 280-380 V, the pressure is 2-6 MPa, the vulcanization time is 6-24 hours, and the liquid hourly space velocity is ⁇ .
  • the hydrogen oil volume ratio is 200-500.
  • the main active component metal, the first co-active component metal, and the second co-active component element in the iron-based hydrogenation catalyst of the present invention are present in the form of an oxide, and after vulcanization treatment It becomes a sulfide form.
  • the hydrotreating temperature is 200-600 ° C
  • the pressure is l-20 MPa
  • the liquid hourly space velocity is 0.1-10 h -
  • the hydrogen oil volume ratio is 100-2000; preferably, the hydrotreating The temperature is 250-400 ° C, the pressure is 2-10 MPa, and the liquid hourly space velocity is ⁇ - ⁇ .
  • the volume ratio of hydrogen oil is 200-1000.
  • the hydrotreating apparatus and method and process flow can be conventionally used in the art for gasoline, diesel, and heavy oil hydrogenation apparatus and processes, and process flows.
  • the hydrotreating can be carried out in one reactor or in a plurality of parallel or series reactors, that is, the catalyst of the present invention can be packed in one reactor or a plurality of reactors in a single process. Hydrotreating is carried out. Without changing the existing gasoline, diesel and heavy oil plus In the case of a hydrogen process, the catalyst of the present invention has a better hydrogenation effect.
  • the iron-based hydrogenation catalyst provided by the present invention uses iron as a main active component metal, zinc and potassium as a first auxiliary component metal, and may include a group selected from the group consisting of IVB, VA, VB, VIB and VIII elements.
  • the second active component element is prepared and matured.
  • the present invention adopts an iron-based catalyst as a hydrogenation catalyst for gasoline, diesel oil and heavy oil, and replaces the molybdenum and tungsten of group VIB as the active component metal, and the cobalt and nickel of group VIII as the metal for gasoline, diesel and Conventional hydrogenation catalyst for heavy oil hydrogenation.
  • the iron-based catalyst of the invention has the advantages of low cost and easy availability of raw materials, simple production process, and the like, and can greatly reduce the production cost of the hydrogenation catalyst, and has a high Gasoline, diesel and heavy oil hydrogenation activities.
  • the iron-based hydrogenation catalyst of the present invention breaks through the limitations of conventional hydrogenation catalysts which have been used for decades as active component metals, and thus has long-term industrial application value.
  • the present embodiment provides a gasoline-diesel iron-based hydrogenation catalyst which is prepared by a dipping method, and the preparation method comprises the following steps:
  • the catalyst semi-finished product was allowed to stand in the air for 20 hours, then dried in an oven at 120 ° C, then heated at a rate of 5 ° C / min, and calcined at 500 ° C for 4 hours in an air atmosphere to obtain a gasoline-diesel iron base.
  • Hydrogenation catalyst FZ-1 Hydrogenation catalyst
  • the total amount of iron, zinc, potassium oxide in the catalyst FZ-1 was measured to be 26% based on the total weight of the catalyst FZ-1.
  • the present embodiment provides a gasoline-diesel iron-based hydrogenation catalyst which is prepared by a coprecipitation method, and the preparation method comprises the following steps:
  • the reaction was stirred in a water bath at 80 ° C for 4 hours, then cooled to 60 ° C and allowed to stand for 24 hours to obtain a precipitate; the precipitate was filtered while hot, washed with deionized water to a pH of about 9, and then Bake in an oven at 120 ° C Dry, further increase at a rate of 5 ° C / min, calcined at 500 ° C, air atmosphere for 2 hours to obtain iron zinc potassium oxide; 4.5g of the iron zinc potassium oxide, 10g pseudo-boehmite (sticky a mixture of 0.4 g of phthalocyanine powder to obtain a mixed powder; a mixed powder is obtained; 0.3 g of citric acid and 0.3 g of nitric acid are dissolved in 10 mL of deionized water to form a peptizing agent; the peptizing agent is added to the mixed powder and kneaded sufficiently.
  • the strip was extruded into a strip having a diameter of 1.5 mm on a extruder, and the strip was dried in an oven at 120 ° C, and then calcined at 500 ° C for 6 hours in an air atmosphere to obtain a gasoline-diesel iron-based hydrogenation catalyst.
  • FZ-2 The strip was extruded into a strip having a diameter of 1.5 mm on a extruder, and the strip was dried in an oven at 120 ° C, and then calcined at 500 ° C for 6 hours in an air atmosphere to obtain a gasoline-diesel iron-based hydrogenation catalyst.
  • the total amount of iron, zinc, potassium oxide in the catalyst FZ-2 was measured to be 31% based on the total weight of the catalyst FZ-2.
  • the present embodiment provides a gasoline-diesel iron-based hydrogenation catalyst which is prepared by a dipping method, and the preparation method comprises the following steps:
  • the impregnating solution was added dropwise to 10 g of an extruded alumina strip having a diameter of 1.5 mm to obtain a catalyst semi-finished product;
  • the catalyst semi-finished product was allowed to stand in the air for 16 hours, then dried in an oven at 120 ° C, then heated at a rate of 5 ° C / min, and calcined at 500 ° C for 8 hours in an air atmosphere to obtain a gasoline-diesel iron base.
  • Hydrogenation catalyst FZ-3 Hydrogenation catalyst
  • the total amount of iron, zinc, potassium and phosphorus oxide in the catalyst FZ-3 was measured to be 30% based on the total weight of the catalyst FZ-3.
  • the present embodiment provides a gasoline-diesel iron-based hydrogenation catalyst which is prepared by a dipping method, and the preparation method comprises the following steps:
  • the impregnating solution was added dropwise to 10 g of an extruded alumina strip having a diameter of 1.5 mm to obtain a catalyst semi-finished product;
  • the catalyst semi-finished product is allowed to stand in the air for 2-24 hours, then dried in an oven at 120 ° C, then heated at a rate of 5 ° C / min, and calcined at 500 ° C for 4 hours in an air atmosphere to obtain gasoline diesel.
  • the total amount of iron, zinc, potassium, vanadium, and phosphorus oxide in the catalyst FZ-4 was measured to be 31% based on the total weight of the catalyst FZ-4.
  • the present embodiment provides a gasoline-diesel hydrogenation catalyst as a comparative catalyst 1, and the preparation method thereof comprises the following steps: 4.74g ammonium metatungstate and 2.26g nickel nitrate were dissolved in 10mL deionized water to prepare an immersion liquid;
  • the impregnating solution was added dropwise to 10 g of an extruded alumina strip having a diameter of 1.5 mm to obtain a catalyst semi-finished product;
  • the catalyst semi-finished product was allowed to stand in the air for 2-24 hours, then dried in an oven at 120 ° C, then heated at a rate of 5 ° C / min, and calcined at 500 ° C for 4 hours in an air atmosphere to obtain a comparative catalyst. 1.
  • the comparative catalyst 1 was found to have a tungsten oxide content of 27% and a nickel oxide content of 4%, based on the total weight of the comparative catalyst 1.
  • This embodiment provides a gasoline-diesel hydrogenation catalyst as a comparative catalyst 2, and the preparation method thereof comprises the following steps:
  • the impregnating solution was added dropwise to 10 g of an extruded alumina strip having a diameter of 1.5 mm to obtain a catalyst semi-finished product;
  • the catalyst semi-finished product was allowed to stand in the air for 14 hours, dried in an oven at 120 ° C, then heated at a rate of 5 ° C / min, and calcined at 500 ° C for 8 hours in an air atmosphere to obtain Comparative Catalyst 2.
  • the total amount of iron oxide in the comparative catalyst 2 was measured to be 31% based on the total weight of the comparative catalyst 2.
  • This embodiment provides a gasoline-diesel hydrogenation catalyst as a comparative catalyst 3, and the preparation method thereof comprises the following steps:
  • the impregnating solution was added dropwise to 10 g of an extruded alumina strip having a diameter of 1.5 mm to obtain a catalyst semi-finished product;
  • the catalyst semi-finished product was allowed to stand in the air for 24 hours, dried in an oven at 120 ° C, then heated at a rate of 5 ° C / min, and calcined at 500 ° C for 2 hours in an air atmosphere to obtain a comparative catalyst 3.
  • the total amount of iron oxide in the comparative catalyst 3 was measured to be 28% based on the total weight of the comparative catalyst 3.
  • This example provides the use of the catalyst of Examples 1-7 for coking diesel oil for hydrotreating.
  • the catalysts of Examples 1-7 were subjected to a sulfurization treatment prior to application to impart hydrogenation activity.
  • the vulcanization is carried out by using a 10 mL high temperature and high pressure hydrogenation microreactor, which is wet in situ vulcanization, that is, wet vulcanization, and the catalyst is not discharged after vulcanization, and the hydrogenation reaction is continued directly in the reactor.
  • the sulfurized oil is a normal bismuth solution containing 5 wt% CS 2 , the vulcanization temperature is 300 ° C, the time is 6 h, the pressure is 4 MPa, the liquid hourly space velocity is lJh- 1 , and the hydrogen oil volume ratio is 300.
  • the hydrotreating of this example was carried out by using a 10 mL high-temperature high-pressure hydrogenation micro-reverse device, and the raw material used was Daqing coking diesel oil.
  • the specific gravity (d) of the coking diesel oil was 0.8196
  • the sulfur content was 1256 ppm
  • the total nitrogen content was 745 ppm.
  • the raw material is pumped by a plunger pump, and the reacted oil sample is cooled by a high separator and collected and analyzed in a low separator.
  • the hydrotreating temperature was 360 ° C
  • the pressure was 6 MPa
  • the liquid hourly space velocity was 1.0 Oh- 1
  • the hydrogen oil volume ratio was 800.
  • the catalyst evaluation results after hydrotreating are shown in Table 1.
  • This example provides the use of the catalysts of Examples 1-7 for hydrotreating catalytic cracking diesel.
  • the catalysts of Examples 1-7 were subjected to a sulfurization treatment prior to application to impart hydrogenation activity.
  • the vulcanization is carried out by using a 10 mL high temperature and high pressure hydrogenation microreactor, which is wet in situ vulcanization, that is, wet vulcanization, and the catalyst is not discharged after vulcanization, and the hydrogenation reaction is continued directly in the reactor.
  • the vulcanized oil is a positive bismuth solution containing 5 wt% CS 2 , the vulcanization temperature is 300 ° C, the time is 10 h, the pressure is 4 MPa, the liquid hourly space velocity is l ⁇ h- 1 , and the hydrogen oil volume ratio is 300.
  • the hydrotreating of the present embodiment is carried out by using a 10 mL high-temperature high-pressure hydrogenation micro-reverse device, and the raw material is Daqing catalytic cracking diesel oil.
  • the specific gravity (df) of the catalytic cracking diesel oil is 0.8796, the sulfur content is 890 ppm, and the total nitrogen content is
  • This example provides the use of the catalysts of Examples 1-7 for hydrotreating fully split FCC gasoline.
  • the catalysts of Examples 1-7 were subjected to a sulfurization treatment prior to application to impart hydrogenation activity.
  • the vulcanization is carried out by using a 10 mL high temperature and high pressure hydrogenation microreactor, which is wet in situ vulcanization, that is, wet vulcanization, and the catalyst is not discharged after vulcanization, and the hydrogenation reaction is continued directly in the reactor.
  • the sulfurized oil is a normal bismuth solution containing 5 wt% CS 2 , the vulcanization temperature is 300 ° C, the time is 6 h, the pressure is 2 MPa, the liquid hourly space velocity is lJh- 1 , and the hydrogen oil volume ratio is 300.
  • the hydrotreating of the present embodiment is carried out by using a 10 mL high-temperature and high-pressure hydrogenation micro-reverse device, and the evaluation of the raw materials is carried out.
  • FCC gasoline has a specific gravity (d) of 0.7296, a sulfur content of 470 ppm, and a research sensitization value (RON) of 92.0.
  • the raw material is pumped by a plunger pump, and the reacted oil sample is cooled by a high separator and collected and analyzed in a low separator.
  • the catalyst evaluation results after hydrotreating are shown in Table 3.
  • the measurement and calculation methods of the desulfurization rate, the denitrification rate, the dearomatization ratio, the RON of the oil, and the gasoline yield of the catalyst are all well-known methods for measurement and calculation in the art.
  • Tables 1, 2 and 3 illustrate that the iron-based hydrogenation catalyst provided by the examples of the present invention has higher hydrodesulfurization, denitrification and dearomatization activities relative to the comparative catalyst. Further, when the iron-based hydrogenation catalyst of the present invention is used for gasoline hydrotreating, the loss of the octal value of the gasoline can be made very low.
  • the iron-based hydrogenation catalyst provided by the examples of the present invention is characterized in that more co-active component elements are introduced, and a catalyst for introducing zinc is introduced with respect to the comparative catalyst 2 which does not introduce the co-active component element at all (comparison The hydrodesulfurization, denitrification and dearomatization rates of the catalyst 3) are several to ten times higher, and the introduction of potassium can further promote the hydrodesulfurization activity of the catalyst in which only zinc is introduced (Comparative Catalyst 3).
  • the iron-based catalyst provided by the examples of the present invention is slightly lower than the conventional supported Ni-W catalyst (Comparative Catalyst 1)
  • the iron-based catalyst provided by the examples of the present invention The main active component metal and the co-active component element (metal) are used at a much lower price than the nickel salt used in the conventional hydrogenation catalyst.
  • Cobalt salt, tungsten salt and molybdenum salt are used at a much lower price than the nickel salt used in the conventional hydrogenation catalyst.
  • the iron-based hydrogenation catalyst provided by the embodiments of the present invention breaks through the limitation of the traditional gasoline-diesel hydrogenation catalyst which has been used for several decades, and has long-term industrial application value.
  • the present embodiment provides a heavy oil iron-based hydrogenation catalyst carrier, and the preparation method thereof comprises the following steps: mixing 10 g of pseudo-boehmite powder and 0.3 g of phthalocyanine powder to obtain a mixed powder;
  • the mixed solution was slowly dropped into the mixed powder, uniformly mixed to form a plastic body, and a strip having a diameter of 1.2 mm was extruded on a extruder;
  • the strip was dried in an oven at 120 ° C, and then calcined at 500 ° C for 4 hours in an air atmosphere to obtain a catalyst carrier.
  • the present embodiment provides a heavy oil iron-based hydrogenation catalyst carrier, and the preparation method thereof comprises the following steps: mixing 7 g of pseudo-boehmite powder, 3 g of MCM-41 molecular sieve, and 0.3 g of phthalocyanine powder to obtain a mixed powder; Nitric acid, 0.3 g of citric acid dissolved in 20 mL of deionized water to obtain a mixed solution;
  • the mixed solution was slowly dropped into the mixed powder, uniformly mixed to form a moldable body, and a strip having a diameter of 1.2 mm was extruded on a extruder;
  • the strip was dried in an oven at 120 ° C, and then calcined at 500 ° C for 4 hours in an air atmosphere to obtain a catalyst carrier.
  • This embodiment provides a heavy oil iron-based hydrogenation catalyst, and the preparation method thereof comprises the following steps:
  • the impregnating solution was slowly added dropwise to 10 g of the catalyst carrier of Example 11 and uniformly mixed to obtain a catalyst semi-finished product; the catalyst semi-finished product was allowed to stand at room temperature for 4 h, then dried in an oven at 120 ° C, and then at 500 ° C, air. The mixture was calcined in an atmosphere for 4 hours to obtain a heavy oil iron-based hydrogenation catalyst Cl.
  • the total amount of iron, zinc and potassium oxide in the heavy iron-based hydrogenation catalyst C1 was determined to be 40%, and the balance was macroporous alumina based on the total weight of the catalyst C1.
  • the specific surface area, pore volume and average pore diameter data of the heavy oil iron-based hydrogenation catalyst C1 are shown in Table 5. Among them, the measurement and calculation methods of the catalyst specific surface area, pore volume and average pore diameter are all well-known methods for measurement and calculation in the art.
  • This embodiment provides a heavy oil iron-based hydrogenation catalyst, and the preparation method thereof comprises the following steps: Mixing 25.30g of iron sulfate, 12.18g of zinc chloride, 0.10g of potassium sulfate and 1.05g of zirconium nitrate, and dissolving in 20mL of deionized water to form an impregnation liquid;
  • the impregnating solution was slowly added dropwise to 10 g of the catalyst carrier of Example 12 and uniformly mixed to obtain a catalyst semi-finished product; the catalyst semi-finished product was allowed to stand at room temperature for 4 h, then dried in an oven at 120 ° C, and then at 500 ° C, air. The mixture was calcined in an atmosphere for 4 hours to obtain a heavy oil iron-based hydrogenation catalyst C2.
  • the total amount of iron, zinc, potassium and zirconium oxide in the heavy oil iron-based hydrogenation catalyst C2 was determined to be 40%, and the balance was macroporous alumina and MCM-41 based on the total weight of the catalyst C2.
  • the specific surface area, pore volume and average pore diameter of the heavy oil iron-based hydrogenation catalyst C2 are shown in Table 5.
  • This embodiment provides a heavy oil iron-based hydrogenation catalyst, and the preparation method thereof comprises the following steps:
  • the impregnating solution was slowly added dropwise to 10 g of the catalyst carrier of Example 12 and uniformly mixed to obtain a catalyst semi-finished product; the catalyst semi-finished product was allowed to stand at room temperature for 8 hours, then dried in an oven at 120 ° C, and then at 500 ° C, air. The mixture was calcined in an atmosphere for 6 hours to obtain a heavy oil iron-based hydrogenation catalyst C3.
  • the total amount of iron, zinc, potassium and zirconium oxide in the heavy oil iron-based hydrogenation catalyst C3 was determined to be 40%, and the balance was macroporous alumina and MCM-41 based on the total weight of the catalyst C3.
  • the specific surface area, pore volume and average pore diameter of the heavy oil iron-based hydrogenation catalyst C3 are shown in Table 5.
  • This embodiment provides a heavy oil iron-based hydrogenation catalyst, and the preparation method thereof comprises the following steps:
  • the total amount of iron, zinc, potassium and titanium oxide in the heavy oil iron-based hydrogenation catalyst C4 is 100% based on the total weight of the catalyst C4.
  • the specific surface area, pore volume and average pore diameter of the heavy oil iron-based hydrogenation catalyst C4 are shown in Table 5.
  • This embodiment provides a heavy oil iron-based hydrogenation catalyst which is prepared by a coprecipitation method, and the preparation method comprises the following steps: Dissolving 32.44 g of ferric chloride and 6.82 g of zinc chloride in 250 mL of deionized water to obtain an aqueous solution of ferric chloride and zinc chloride; dissolving 8 g of potassium hydroxide in 80 mL of deionized water to obtain a potassium hydroxide solution; stirring While slowly adding potassium hydroxide solution to an aqueous solution of ferric chloride and zinc chloride;
  • the reaction was stirred in a water bath at 80 ° C for 4 hours, then cooled to 60 ° C and allowed to stand for 24 hours to obtain a precipitate; the precipitate was filtered while hot, washed with deionized water to a pH of about 9, and then Drying in an oven at 120 ° C, heating at a rate of 5 ° C / min, calcining at 500 ° C, air atmosphere for 2 hours, to obtain iron zinc potassium oxide; 6.0 g iron zinc potassium oxide, 10 g Boehmite (binder), 0.4 g of phthalocyanine powder is mixed into a uniform powder to obtain a mixed powder; 0.3 g of citric acid and 0.3 g of nitric acid are dissolved in 10 mL of deionized water to form a peptizing agent; The powder was mixed and kneaded sufficiently, and extruded into a strip having a diameter of 1.5 mm on a extruder, and the strip was dried in an oven at 120 ° C
  • the total amount of iron, zinc, potassium oxide in the catalyst C5 was measured to be 40% based on the total weight of the catalyst C5.
  • the specific surface area, pore volume and average pore diameter of the heavy iron-based hydrogenation catalyst C5 are shown in Table 5.
  • This embodiment provides a comparative catalyst, and the preparation method thereof comprises the following steps:
  • the impregnating solution was slowly added dropwise to 10 g of the catalyst carrier of Example 11 and uniformly mixed to obtain a catalyst semi-finished product; the catalyst semi-finished product was allowed to stand at room temperature for 4 h, then dried in an oven at 120 ° C, and then at 500 ° C, air. The mixture was calcined under an atmosphere for 4 hours to obtain a comparative catalyst C6.
  • the total amount of iron oxide in the comparative catalyst C6 was measured to be 40%, and the balance was macroporous alumina based on the total weight of the catalyst C6.
  • the specific surface area, pore volume and average pore diameter of the comparative catalyst C6 are shown in Table 5.
  • This embodiment provides a comparative catalyst, and the preparation method thereof comprises the following steps:
  • the impregnating solution was slowly added dropwise to 10 g of the catalyst carrier of Example 12 and uniformly mixed to obtain a catalyst semi-finished product; the catalyst semi-finished product was allowed to stand at room temperature for 4 h, then dried in an oven at 120 ° C, and then at 500 ° C, air. The mixture was calcined under an atmosphere for 4 hours to obtain a comparative catalyst C7.
  • the total amount of iron zinc oxide in the comparative catalyst C7 was measured to be 40%, and the balance was macroporous alumina and MCM-41 based on the total weight of the catalyst C7.
  • the specific surface area, pore volume and average pore diameter of the comparative catalyst C7 are shown in Table 5.
  • This embodiment provides a comparative catalyst, and the preparation method thereof comprises the following steps:
  • the impregnating solution was slowly added dropwise to 10 g of the catalyst carrier of Example 12 and uniformly mixed to obtain a catalyst semi-finished product; the catalyst semi-finished product was allowed to stand at room temperature for 4 h, then dried in an oven at 120 ° C, and then at 500 ° C, air. The mixture was calcined in an atmosphere for 4 hours to obtain a heavy oil hydrogenation catalyst C8.
  • the total amount of tungsten nickel oxide in the comparative catalyst C8 was measured to be 20%, and the balance was macroporous alumina and MCM-41 based on the total weight of the catalyst C8.
  • the specific surface area, pore volume and average pore diameter of the comparative catalyst C8 are shown in Table 5.
  • This example provides the use of the catalysts of Examples 13-20 for hydrotreating atmospheric residue.
  • the catalysts of Examples 13-20 were subjected to a sulfurization treatment prior to application to impart hydrogenation activity.
  • the vulcanization is carried out by using a 50 mL high temperature and high pressure hydrogenation microreactor, which is wet in situ vulcanization, that is, wet vulcanization, and the catalyst is not discharged after vulcanization, and the hydrogenation reaction is continued directly in the reactor.
  • the vulcanized oil is a normal bismuth solution containing 5 wt% CS 2 , the vulcanization temperature is 300 ° C, the time is 10 h, the pressure is 4 MPa, and the liquid hourly space velocity is ⁇ ⁇ ⁇ ⁇ ⁇ hydrogen oil volume ratio is 300.
  • the hydrotreating of this example was carried out using a 50 mL high temperature and high pressure hydrogenation microreactor, and the evaluation raw material was a sand atmospheric residue (the properties of which are shown in Table 4).
  • the raw material is pumped by a plunger pump, and the reacted oil sample is cooled by a high separator and collected and analyzed in a low separator.
  • the hydrotreating temperature is 400 ° C
  • the pressure is 10 MPa
  • the liquid hourly space velocity is 1.0 Oh- 1
  • the hydrogen oil volume ratio is 1000.
  • the catalyst evaluation results after hydrotreating are shown in Table 5.
  • Catalyst C1 C2 C3 C4 C5 C6 C7 C8 Specific surface area, m 2 /g 170 315 325 71 102 324 173 357 Pore volume, cc/g 0.77 0.98 0.92 0.32 0.67 0.93 0.76 1.01 Average pore size, nm 11.9 9.0 11.4 8.0 8.2 9.4 12.3 11.1 Desulfurization rate, % 50.4 54.1 55.0 55.2 49.8 7.9 47.1 67.0 Denitrification rate, % 31.8 32.9 34.1 33.8 31.0 5.1 30.5 40.2 Example 22
  • This example provides the use of the catalyst-focused wax oil of Example 15, Example 16, Example 19 and Example 20 for hydrotreating.
  • the catalysts of Examples 15, 16, 19, and 20 were subjected to a vulcanization treatment before application to give the catalyst a better hydrogenation effect.
  • the vulcanization is carried out by using a 50 mL high temperature and high pressure hydrogenation microreactor, which is wet in situ vulcanization, that is, wet vulcanization, and the catalyst is not discharged after vulcanization, and the hydrogenation reaction is continued directly in the reactor.
  • the vulcanized oil is a positive bismuth solution containing 5 wt% CS 2 , the vulcanization temperature is 400 ° C, the time is 8 h, the pressure is 5 MPa, the liquid hourly space velocity is 1.511 -1 , and the hydrogen oil volume ratio is 300.
  • the hydrotreating of this example was carried out by using a 50 mL high-temperature high-pressure hydrogenation micro-reverse device, and the evaluation raw material was Dagang coking wax oil, and the sulfur content was 0.253 wt%, and the total nitrogen content was 0.51 wt%.
  • the raw material is pumped by a plunger pump, and the reacted oil sample is cooled by a high separator and collected and analyzed in a low separator.
  • the hydrotreating temperature was 360 ° C
  • the pressure was 6 MPa
  • the liquid hourly space velocity was lh- 1
  • the hydrogen oil volume ratio was 500.
  • This example provides the use of the catalysts of Example 15, Example 16, Example 19 and Example 20 for hydrotreating a vacuum residue.
  • the catalysts of Examples 15, 16, 19, and 20 were subjected to a vulcanization treatment before application to give the catalyst a better hydrogenation effect.
  • the vulcanization is carried out by using a 50 mL high temperature and high pressure hydrogenation microreactor, which is wet in situ vulcanization, that is, wet vulcanization, and the catalyst is not discharged after vulcanization, and the hydrogenation reaction is continued directly in the reactor.
  • the vulcanized oil is a normal bismuth solution containing 5 wt% CS 2 , the vulcanization temperature is 360 ° C, the time is 12 h, the pressure is 4 MPa, the liquid hourly space velocity is 21 ⁇ , and the hydrogen oil volume ratio is 300.
  • the hydrotreating of this example was carried out using a 50 mL high temperature and high pressure hydrogenation microreactor, and the evaluation raw material was a sand vacuum residue (the properties of which are shown in Table 7).
  • the raw material is pumped by a plunger pump, and the reacted oil sample is cooled by a high separator and collected and analyzed in a low separator.
  • the hydrotreating temperature was 360 ° C
  • the pressure was 8 MPa
  • the liquid hourly space velocity was lh- 1
  • the hydrogen oil volume ratio was 800.
  • the results of Tables 5, 6 and 8 show that the heavy oil iron-based hydrogenation catalyst of the examples of the present invention has high heavy oil hydrodesulfurization, denitrification and demetallization activity.
  • the iron-based hydrogenation catalyst of the embodiment of the present invention is characterized in that a co-active component element (metal) is introduced, and a catalyst for introducing zinc is introduced with respect to the comparative catalyst C6 in which the co-active component element (metal) is not introduced at all.
  • the hydrodesulfurization rate of Comparative Catalyst C7 was increased several times, and the introduction of potassium further promoted the hydrodesulfurization activity of the catalyst in which only zinc was introduced (Comparative Catalyst C7).
  • the desulfurization, denitrification rate, and metal removal rate of the catalyst of the examples of the present invention are slightly lower than the conventional supported Ni-W catalyst (Comparative Catalyst C8), the active component metal used in the catalyst of the embodiment of the present invention
  • the price of the metal and the promoter metal is much lower than that of the conventional hydrogenation catalyst, such as nickel salt, cobalt salt, tungsten salt and molybdenum salt.
  • the iron-based hydrogenation catalyst of the embodiment of the present invention breaks through the limitation of the conventional hydrogenation catalyst which has been used for several decades, and has important theoretical research value and industrial application value.

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Abstract

本发明涉及一种铁基加氢催化剂,该铁基加氢催化剂以铁作为主活性组分金属,以锌和钾为第一助活性组分金属;其中,所述主活性组分金属和所述第一助活性组分金属的摩尔比为0.5-200:1。本发明的铁基加氢催化剂突破了传统加氢催化剂沿用数十年的活性组分金属的限制,因此具有长远的工业应用价值。

Description

一种铁基加氢催化剂及其应用 技术领域
本发明涉及一种铁基加氢催化剂及其应用,属于石油炼制领域中的加氢催化剂技术 领域。
背景技术
自从 1926年世界上第一套后来被称为 "古典加氢"的技术在德国工业化以来, 加 氢工艺已经走过了近一个世纪的历程。特别是近五十年来, 加氢作为多产汽油、 柴油和 其他优质中间熘分油的一种重要手段, 得到了很大的重视和发展, 其间相继涌现出了许 多新的加氢催化剂及其制备方法。
US3779903通过将镍盐、钨盐浸渍到经过干燥、焙烧的氧化铝溶胶制得的特殊载体 上, 再进一步干燥、 焙烧, 制得以氧化钨为主要活性成分, 氧化镍为助活性成分, 氟为 助剂的加氢催化剂。 US4330395公开了一种将镍盐浸渍到以铝化合物和钨化合物为原料 制得的载体上的加氢催化剂的制备方法,得到的催化剂在使用前可用硫化合物和氟化合 物进行活化, 取得较好的中间熘分油加氢处理效果。 CN101439289A公开了一种以尿素 或氨水为反应助剂, 采用载体孔内原位反应的方法使金属活性组分生成钼酸镍(钴)或 钨酸镍(钴)类化合物, 从而可以避免金属与载体的反应, 使得活性组分更易被硫化, 提高了加氢催化剂的活性。
由于包括上述现有技术的加氢催化剂在内的传统负载型催化剂中的载体没有活性 或活性不高, 且载体所占比例很大, 从而导致负载型催化剂的催化活性难以满足生产超 低硫柴油的要求。所以, 近年来出现了摒弃传统加氢催化剂中必不可少的载体, 而直接 以本身含有孔结构的镍、钴、钨、钼的氧化物或硫化物作为主要组成的非负载型(Bulk) 催化剂。 US6582590公布了采用直接沉淀法制备非负载型加氢催化剂的方法, 该方法是 将可溶性钼酸盐和钨酸盐溶于水后与碱液混合, 再将可溶性镍盐溶于水并在 90°C下保 持, 而后以一定速度加入钼、 钨酸盐的碱溶液, 最终经过过滤、 干燥制得非负载型加氢 脱硫催化剂。 US6712955、 US6156695 , US6783663也公开了类似的非负载型加氢催化 剂的制备方法, 这些技术全部使用 VIII族的钴、 镍和 vm族的钼、 钨中的一种或两种 的组合作为活性组分金属。 CN101255356A也公布了一种通过尿素熔融反应制备自身具 有纳米孔道和较高比表面积的镍 (钴) -钨 (钼) 非负载型催化剂的制备方法, 使用该 方法制得的催化剂具有较好的加氢处理活性。
另一方面, 由于重质油 (重油)产量和原油中的重质成分日益增多, 加氢作为加工 重质油的一种重要手段得到了越来越大的重视和发展。近年来, 在业内人士的关注和研 究中, 相继涌现出了许多新的重油加氢催化剂及其制备方法。
CN1086534A 公开了一种重油加氢脱氮催化剂及其制法。 该催化剂的组成为 W-Mo-Ni/Si02-B203-Al203。 CN1458236A公开了一种重油加氢脱金属、脱硫催化剂, 该 催化剂的活性组分含有 lwt%-20wt%的氧化钨和 /或氧化钼, 0.5wt%-5.0wt%的氧化镍和 / 或氧化钴, 助剂含有 0.1wt%-3.0wt%的碱金属和 /或碱土金属氧化物。该方法制备的催化 剂同时具有较高的脱金属活性和脱硫活性, 并且活性稳定性较高, 特别是脱硫活性的稳 定性较好。 CN1110304A公开了一种重油加氢处理催化剂, 该催化剂以含硅和磷的氧化 铝为载体,担载钼、镍、磷元素。该催化剂含有 10-30wt%MoO3、 2-6wt%NiO、 2-6wt%P, 其表现出良好的脱氮性能。 USP727980公开了一种加氢脱金属催化剂及其制备方法, 该 催化剂是以一种烧结型氧化物(A1203, Si02, Ti02或其混合物) 为载体, 首先浸渍硝 酸铁, 然后经干燥、 焙烧后, 再浸渍钼酸铵溶液, 之后进一步进行干燥、 熔烧而得到的 存在两种晶相的成品催化剂。该催化剂的金属含量高, 加氢活性高, 但是该催化剂具有 制备工艺复杂, 价格昂贵等缺点。
此外, 在重油加氢处理过程中, 由于重油粘度高且杂质含量高, 因此重油加氢处理 过程的空速很小, 所以催化剂的用量相较于其它炼油过程大大增加, 并且重油加氢处理 的催化剂使用寿命短, 可再生性差, 因此降低催化剂的成本尤为重要。现有的降低重油 加氢催化剂成本的途径一般是使用廉价载体或者采用简便易行的制备方法。 CN102039140A公开了一种重油加氢处理催化剂及其制备方法, 主要采用廉价的天然粘 土如高岭土、 蒙脱土、 硅藻土和天然白土等作为载体的一部分。 该粘土以 Si02的量计 占催化剂重量的 0.5wt%-30wt%, 得到的催化剂既具有与以纯氧化铝做载体的催化剂相 当的加氢活性, 又具有价格低廉的优势。 CN1289821A公开了一种高活性渣油加氢转化 催化剂及其制备方法。该催化剂的制备是采用完全混捏法, 以鈦作为助剂, 把氢氧化铝 干胶粉和分子筛按一定比例混合, 然后先加入 VIB族金属的碱性溶液, 再加入 VIII族 和 /或 VIB 族金属的酸性溶液。 该催化剂的孔容为 0.36-0.60mL/g, 比表面积为 190-280m2/g。由于该方法采用了简便易行的混捏制备法,所以相较于浸渍法和沉淀法成 本较低。
由此可见,虽然多年以来,研究者们在汽柴油和重油负载型催化剂载体和助剂改性、 以及近年出现的突破性的非负载型催化剂的制备方面做了大量研究工作, 同时为了降低 催化剂生产制备成本, 也做了很多努力。 但是以镍、 钴作为助剂, 钼、 钨作为主要活性 组分金属的基本组合并未被打破。并且, 上述所有现有技术的制备方法的共同缺点仍为 成本较高, 其根本原因在于作为活性金属的镍、 钴、 钼和钨在地壳中并非大量存在, 它 们的价格非常昂贵。
综上所述, 研发出一种制作成本低廉的汽柴油和重油加氢催化剂, 仍是本领域亟待 解决的问题之一。
发明内容
为解决上述技术问题, 本发明的目的在于提供一种适用于汽油、柴油和重油等的铁 基加氢催化剂及其应用。本发明的铁基加氢催化剂以铁为主活性组分金属, 以锌和钾为 第一助活性组分金属, 具有制作成本低廉, 制作工艺简单的优点。
为达到上述目的, 本发明提供了一种铁基加氢催化剂, 其中, 该铁基加氢催化剂以 铁作为主活性组分金属, 以锌和钾为第一助活性组分金属(也可称为第一助活性组分元 素); 以该铁基加氢催化剂的总重量为基准, 所述主活性组分金属和助活性组分元素的 总量为 5-100%, 余量为粘结剂或载体, 以氧化物形式计; 所述助活性组分元素包括第 一助活性组分金属;
其中, 所述主活性组分金属和所述第一助活性组分金属的摩尔比为 0.5-200: 1 (优 选为 0.8-20: 1 ) 。
根据本发明的具体实施方案, 优选地, 上述铁基加氢催化剂还包括选自 IVB、 VA、 VB、 VIB和 VIII族元素的第二助活性组分元素, 其中, IVB元素优选为鈦、锆, V A元 素优选为磷, VB元素优选为钒, VIB元素优选为铬, VIII族元素优选为钴、 镍、 钯和 铂; 主活性组分金属与第二助活性组分元素的摩尔比为 0.5-200: 1, 优选为 5-100: 1; 以该铁基加氢催化剂的总重量为基准,主活性组分金属和助活性组分元素的总量为 5-100%, 余量为粘结剂或载体, 以氧化物形式计; 所述助活性组分元素包括第一助活性 组分金属和第二助活性组分元素。
催化剂中的主活性组分金属、助活性组分元素(金属) 的总含量的测定及计算方法 均可以采用本领域公知的测定及计算方法, 均以氧化物的形式计算。
本发明提供的上述铁基加氢催化剂可以仅由主活性组分金属、助活性组分元素(可 以是单独的第一助活性组分金属,也可以是第一助活性组分金属和第二助活性组分元素 的组合)组成, 而不包含粘结剂和载体, 即主活性组分金属和助活性组分元素的总量为 100%的情况, 这种组成的铁基加氢催化剂可以通过压片成型法制成, 即将主活性组分 金属和助活性组分元素混合之后直接压片成型。
上述铁基加氢催化剂也可以是由主活性组分金属、助活性组分元素、粘结剂或载体 等三部分组成, 采用粘结剂的铁基加氢催化剂可以通过共沉淀法制备, 采用载体的铁基 加氢催化剂可以通过浸渍法制备。对于具有这种组成的铁基加氢催化剂, 优选地, 以该 铁基加氢催化剂的总重量为基准, 主活性组分金属和助活性组分元素的总量为 20-70% (更优选 20-50%) , 余量为粘结剂或载体, 以氧化物形式计, 所述助活性组分元素包 括第一助活性组分金属或者第一助活性组分金属和第二助活性组分元素的组合。
根据本发明的具体实施方案, 优选地, 上述铁基加氢催化剂是由浸渍法、共沉淀法 或压片成型法制备得到的。
根据本发明的具体实施方案, 优选地, 所述浸渍法包括以下步骤:
将主活性组分金属的盐、 第一助活性组分金属的盐溶于去离子水中, 配成浸渍液; 将浸渍液加入到载体中, 得到催化剂半成品;
将催化剂半成品在空气中静置 2-24小时, 然后烘干, 再在空气气氛、 200-800°C焙 烧 2-8h, 得到铁基加氢催化剂。
在上述的浸渍法中, 优选地, 当铁基加氢催化剂含有第二助活性组分元素时, 第二 助活性组分元素的盐与主活性组分金属的盐、第一助活性组分金属的盐一起溶于去离子 水中。
在上述的浸渍法中, 优选地, 所述浸渍液的体积与载体的饱和吸水量相同。
在上述的浸渍法中, 优选地, 所述催化剂半成品的烘干是在 120°C的烘箱中进行。 在上述的浸渍法中, 优选地, 所述催化剂半成品在进行焙烧时是以 5°C/min的速率 进行升温。
根据本发明的具体实施方案, 优选地, 所采用的载体包括黄铁矿(FeS2) 、 磁黄铁 矿(Fei_xS) 、 三氧化二铁、 四氧化三铁、 氧化铝、 二氧化硅、 无定形硅铝和沸石分子 筛等中的一种或几种的组合。
根据本发明的具体实施方案, 优选地, 所述共沉淀法包括以下步骤:
将主活性组分金属的盐和第一助活性组分元素的盐的水溶液以及沉淀剂的水溶液 混合均匀;
然后在 40-95Ό水浴中搅拌反应 l-24h, 再在 40-95 °C水浴中静置老化 2-48h, 得到 沉淀物;
将沉淀物进行过滤、 水洗、 烘干后, 得到催化剂前驱体;
将催化剂前驱体在空气气氛、 200-800°C焙烧 2-8h, 得到金属氧化物;
将金属氧化物与粘结剂混合进行成型处理, 得到铁基加氢催化剂。
在上述的共沉淀法中, 优选地, 当铁基加氢催化剂含有第二助活性组分元素时, 所 述第二助活性组分元素的盐与主活性组分金属的盐、第一助活性组分金属的盐一起与沉 淀剂的水溶液混合。
在上述的共沉淀法中, 优选地, 所述成型处理可以为挤条成型或混捏成型。 在成型 处理的过程中, 可以采用常规使用的田菁粉等作为助挤剂, 柠檬酸、 醋酸、 硝酸等作为 胶溶剂, 与金属氧化物和粘结剂混合后进行挤条或混捏等成型操作。
根据本发明的具体实施方案, 优选地, 所述共沉淀法还包括以下步骤: 将成型处理 后得到的铁基加氢催化剂进行进一步的焙烧; 更优选地, 该焙烧的条件为: 以 5°C/min 的升温速率进行升温, 在空气气氛、 200-800°C下焙烧 2-8h。
根据本发明的具体实施方案, 优选地, 本发明的铁基加氢催化剂所采用的粘结剂包 括氧化铝、硅溶胶、 铝溶胶、 水玻璃等中的一种或几种的组合。 粘结剂的用量可以根据 铁基加氢催化剂的成分组成确定, 一般可以控制为铁基加氢催化剂总重量的 10%-95%。
在上述的共沉淀法中, 将所述沉淀物进行过滤、 水洗、 烘干后, 还可以视情况进行 粉碎, 而后将得到的催化剂前驱体进行焙烧。
在上述的共沉淀法中, 优选地, 所述沉淀物的烘干是在 120°C的烘箱中进行。
在上述的共沉淀法中, 优选地, 所述催化剂前驱体在进行焙烧时是以 5°C/min的速 率进行升温。
在上述的共沉淀法中, 优选地, 所述沉淀剂包括 NaOH、 KOH、 Na2C03、 K2C03、 Na2S、 (NH4)2S、 尿素和氨水等中的一种或几种的组合, 所述沉淀剂与所述主活性组分 金属、所述第一助活性组分金属、 所述第二助活性组分元素的摩尔比为 1-6: 1, 即沉淀 剂的摩尔量与三者的摩尔量之和的比例。 当采用氨水作为沉淀剂时, 可以直接使用, 无 需配制沉淀剂的水溶液。
在上述的共沉淀法中,主活性组分金属的盐和助活性组分元素的盐的水溶液的浓度 以及沉淀剂的水溶液的浓度可以由本领域技术人员进行常规的调控,只要能够满足上述 的比例关系并能使反应顺利进行即可。
并且,主活性组分金属的盐和助活性组分元素的盐的水溶液可以为主活性组分金属 的盐和助活性组分元素的盐分别溶于去离子水中再混合而成的水溶液,也可以为主活性 组分金属的盐和助活性组分元素的盐同时溶于去离子水中而形成的水溶液。将主活性组 分金属的盐和助活性组分元素的盐的水溶液以及沉淀剂的水溶液混合均匀的具体操作 可以为将沉淀剂的水溶液加入到主活性组分金属的盐和助活性组分元素的盐的水溶液 中并搅拌均匀。
根据本发明的具体实施方案, 优选地, 所述压片成型法包括以下步骤:
将主活性组分金属的盐、第一助活性组分金属的盐混合均匀, 然后烘干, 再在空气 气氛、 200-800°C焙烧 2-8h, 得到铁基加氢催化剂的氧化物粉末;
将铁基加氢催化剂的氧化物粉末加入压片机中压片成型, 得到铁基加氢催化剂。 在上述压片成型法中, 优选地, 当铁基加氢催化剂含有第二助活性组分元素时, 第 二助活性组分元素的盐与主活性组分金属的盐、 第一助活性组分金属的盐一起混合。
在上述的浸渍法、 共沉淀法和压片成型法中, 优选地, 所述主活性组分金属的盐包 括硝酸铁、 硫酸铁、 氯化铁和磷酸铁等中的一种或几种的组合。
在上述的浸渍法、 共沉淀法和压片成型法中, 优选地, 所述第一助活性组分金属的 盐包括硝酸盐、 硫酸盐、 氯化盐和磷酸盐等中的一种或几种的组合。
在上述的浸渍法、 共沉淀法和压片成型法中, 优选地, 所述第二助活性组分元素的 盐包括硝酸盐、 硫酸盐、 氯化盐和磷酸盐等中的一种或几种的组合。
本发明还提供上述的汽油柴油和重油铁基加氢催化剂在直熘汽油、 直熘柴油、 焦化 汽油、 焦化柴油、 催化裂化汽油、 催化裂化柴油以及常压渣油、 减压渣油、 煤焦油、 脱 沥青油以及从油砂或页岩中提取的重质油中的一种或几种的混合油的加氢处理中的应 用。 所述加氢处理可以包括加氢脱硫、 加氢脱氮、 芳烃的加氢饱和和加氢脱金属等。
本发明的铁基加氢催化剂在通过上述浸渍法、 共沉淀法或压片成型法制备得到后, 经过硫化处理可以达到高活性。硫化处理可以采用本领域常规的加氢催化剂的硫化技术 进行, 所采用的硫化油或硫化剂等也可以为本领域常规使用的硫化油或硫化剂等。硫化 处理的温度可以为 200-450°C, 压力可以为 0.1-10MPa, 时间可以为 2-48小时, 液时空 速可以为 O.l Oh—1, 氢油体积比可以为 100-800; 优选地, 硫化处理的温度为 280-380 V , 压力为 2-6MPa, 硫化处理的时间为 6-24小时, 液时空速为 Ι^ΙιΛ 氢油体积比为 200-500
在进行硫化处理之前, 本发明的铁基加氢催化剂中的主活性组分金属、 第一助活性 组分金属、 第二助活性组分元素是以氧化物形式存在的, 经过硫化处理之后会变成硫化 物形式。
在上述的应用中, 优选地, 加氢处理的温度为 200-600°C, 压力为 l-20MPa, 液时 空速为 0.1-10h— 氢油体积比为 100-2000; 优选地, 加氢处理的温度为 250-400°C, 压 力为 2-10MPa, 液时空速为 Ο^-δΙιΛ 氢油体积比为 200-1000。
在上述的应用中, 加氢处理的装置和方法以及工艺流程可以为本领域常规的汽油、 柴油和重油加氢的装置和方法以及工艺流程。 该加氢处理可以在一个反应器中进行, 也 可以在多个并联或串联反应器中进行, 也就是说, 本发明的催化剂可以装填在一套流程 中的一个反应器或者多个反应器中进行加氢处理。 在不改变现有的汽油、 柴油和重油加 氢工艺流程的情况下, 本发明的催化剂具有较好的加氢效果。
本发明所提供的铁基加氢催化剂采用铁作为主活性组分金属, 以锌和钾为第一助活 性组分金属, 并且可以包括选自 IVB、 VA、 VB、 VIB和 VIII族元素的第二助活性组分 元素, 其制备方法成熟且简单。
本发明首次采用铁基催化剂作为汽油、柴油和重油的加氢催化剂,替代了以 VIB族 的钼、钨作为活性组分金属、 以 VIII族的钴、镍作为助金属的用于汽油、柴油和重油加 氢的传统加氢催化剂。相较于传统的汽油、 柴油和重油加氢催化剂, 本发明的铁基催化 剂具有原料廉价易得、制作工艺简单等优点, 在能够大大降低加氢催化剂的生产成本的 同时, 还具有较高的汽油、 柴油和重油加氢活性。
本发明的铁基加氢催化剂突破了传统加氢催化剂沿用数十年的活性组分金属的限 制, 因此具有长远的工业应用价值。
具体实施方式
下面结合实施例, 对本发明的技术方案及技术效果做进一步的详细说明, 但不能理 解为对本发明可实施范围的限定。
实施例 1
本实施例提供一种汽油柴油铁基加氢催化剂, 其为采用浸渍法制备得到的, 该制备 方法包括以下步骤:
将 15.18g硝酸铁、 3.65g硝酸锌及 0.05g硝酸钾溶于 10mL去离子水中配成浸渍液; 将该浸渍液逐滴加入到 10g挤条成型的直径为 1.5mm的氧化铝条中, 得到催化剂 半成品;
将催化剂半成品在空气中静置 20小时, 再于 120°C的烘箱中烘干, 然后以 5°C/min 的速率升温, 在 500°C、 空气气氛下焙烧 4小时, 得到汽油柴油铁基加氢催化剂 FZ-1。
测得催化剂 FZ-1中铁锌钾氧化物的总量为 26%,以该催化剂 FZ-1的总重量为基准。 实施例 2
本实施例提供一种汽油柴油铁基加氢催化剂, 其为采用共沉淀法制备得到的, 该制 备方法包括以下步骤:
将 32.44g氯化铁和 6.82g氯化锌溶于 250mL去离子水中, 得到氯化铁和氯化锌的 水溶液; 将 8g氢氧化钾溶于 80mL去离子水中, 得到氢氧化钾溶液; 边搅拌边将氢氧 化钾溶液缓慢加入到氯化铁和氯化锌的水溶液中;
在 80°C的水浴中搅拌反应 4小时,接着降温至 60°C静置老化 24小时,得到沉淀物; 将该沉淀物趁热过滤,用去离子水洗涤至 pH值约等于 9,然后于 120°C的烘箱中烘 干, 再以 5°C/min的速率升温, 在 500°C、 空气气氛下焙烧 2小时, 得到铁锌钾氧化物; 将 4.5g该铁锌钾氧化物, 10g拟薄水铝石(粘结剂), 0.4g田菁粉混合成均匀粉末, 得到混合粉末; 将 0.3g柠檬酸和 0.3g硝酸溶于 10mL去离子水中, 形成胶溶剂; 将该 胶溶剂加入该混合粉末并充分捏合, 在挤条机上挤成直径 1.5mm 的条状物, 将该条状 物在 120°C的烘箱中烘干, 然后在 500°C、 空气气氛下焙烧 6小时, 得到汽油柴油铁基 加氢催化剂 FZ-2。
测得催化剂 FZ-2中铁锌钾氧化物的总量为 31%,以该催化剂 FZ-2的总重量为基准。 实施例 3
本实施例提供一种汽油柴油铁基加氢催化剂, 其为采用浸渍法制备得到的, 该制备 方法包括以下步骤:
将 14.56g硫酸铁、 4.78g硝酸锌、 0.04g硝酸钾和 0.08g磷酸溶于 10mL去离子水中, 配成浸渍液;
将该浸渍液逐滴加入到 10g挤条成型的直径为 1.5mm的氧化铝条中, 得到催化剂 半成品;
将催化剂半成品在空气中静置 16小时, 再于 120°C的烘箱中烘干, 然后以 5°C/min 的速率升温, 在 500°C、 空气气氛下焙烧 8小时, 得到汽油柴油铁基加氢催化剂 FZ-3。
测得催化剂 FZ-3中铁锌钾磷氧化物的总量为 30%,以催化剂 FZ-3的总重量为基准。 实施例 4
本实施例提供一种汽油柴油铁基加氢催化剂, 其为采用浸渍法制备得到的, 该制备 方法包括以下步骤:
将 13.98g磷酸铁、 6.65g氯化锌、 0.09g硝酸钾和 0.35g偏钒酸铵溶于 10mL去离子 水中, 配成浸渍液;
将该浸渍液逐滴加入到 10g挤条成型的直径为 1.5mm的氧化铝条中, 得到催化剂 半成品;
将催化剂半成品在空气中静置 2-24小时,再于 120°C的烘箱中烘干,然后以 5°C/min 的速率升温, 在 500°C、 空气气氛下焙烧 4小时, 得到汽油柴油铁基加氢催化剂 FZ-4。
测得该催化剂 FZ-4中铁锌钾钒磷氧化物的总量为 31%,以该催化剂 FZ-4的总重量 为基准。
实施例 5
本实施例提供一种汽油柴油加氢催化剂, 作为对比催化剂 1, 其制备方法包括以下 步骤: 将 4.74g偏钨酸铵和 2.26g硝酸镍溶于 10mL去离子水中, 配成浸渍液;
将该浸渍液逐滴加入到 10g挤条成型的直径为 1.5mm的氧化铝条中, 得到催化剂 半成品;
将催化剂半成品在空气中静置 2-24小时,再于 120°C的烘箱中烘干,然后以 5°C/min 的速率升温, 在 500°C、 空气气氛下焙烧 4小时, 得到对比催化剂 1。
测得该对比催化剂 1中氧化钨的含量为 27%, 氧化镍的含量为 4%, 均以该对比催 化剂 1的总重量为基准。
实施例 6
本实施例提供一种汽油柴油加氢催化剂, 作为对比催化剂 2, 其制备方法包括以下 步骤:
将 20.05g硝酸铁溶于 10mL去离子水中, 配成浸渍液;
将该浸渍液逐滴加入到 10g挤条成型的直径为 1.5mm的氧化铝条中, 得到催化剂 半成品;
将催化剂半成品在空气中静置 14小时, 再于 120°C的烘箱中烘干, 然后以 5°C/min 的速率升温, 在 500°C、 空气气氛下焙烧 8小时, 得到对比催化剂 2。
测得该对比催化剂 2中铁氧化物的总量为 31%,以该对比催化剂 2的总重量为基准。 实施例 7
本实施例提供一种汽油柴油加氢催化剂, 作为对比催化剂 3, 其制备方法包括以下 步骤:
将 14.56g硫酸铁、 4.78g硝酸锌溶于 10mL去离子水中, 配成浸渍液;
将该浸渍液逐滴加入到 10g挤条成型的直径为 1.5mm的氧化铝条中, 得到催化剂 半成品;
将催化剂半成品在空气中静置 24小时, 再于 120°C的烘箱中烘干, 然后以 5°C/min 的速率升温, 在 500°C、 空气气氛下焙烧 2小时, 得到对比催化剂 3。
测得该对比催化剂 3中铁氧化物的总量为 28%,以该对比催化剂 3的总重量为基准。 实施例 8
本实施例提供实施例 1-7的催化剂对焦化柴油进行加氢处理的应用。
实施例 1-7 的催化剂在应用前均进行了硫化处理, 使其具有加氢活性。 硫化采用 lOmL高温高压加氢微反装置进行, 其为湿法原位硫化, 即采用湿法硫化, 且硫化后催 化剂不卸出, 直接在反应器中继续进行加氢反应。硫化油为含 5wt% CS2的正癸垸溶液, 硫化的温度为 300°C, 时间为 6h,压力为 4MPa,液时空速为 lJh—1,氢油体积比为 300。 本实施例的加氢处理采用 10mL高温高压加氢微反装置进行, 评价原料采用大庆焦 化柴油, 该焦化柴油的比重 (d )为 0.8196, 硫含量为 1256ppm, 总氮含量为 745ppm。 原料采用柱塞泵泵入, 反应后的油样经高分离器冷却后, 在低分离器采集分析。 加氢处 理的温度为 360°C, 压力为 6MPa, 液时空速为 l.Oh—1, 氢油体积比为 800。 加氢处理后 的催化剂评价结果如表 1所示。
实施例 9
本实施例提供实施例 1-7的催化剂对催化裂化柴油进行加氢处理的应用。
实施例 1-7 的催化剂在应用前均进行了硫化处理, 使其具有加氢活性。 硫化采用 lOmL高温高压加氢微反装置进行, 其为湿法原位硫化, 即采用湿法硫化, 且硫化后催 化剂不卸出, 直接在反应器中继续进行加氢反应。硫化油为含 5wt% CS2的正癸垸溶液, 硫化的温度为 300°C,时间为 10h,压力为 4MPa,液时空速为 l^h—1,氢油体积比为 300。
本实施例的加氢处理采用 10mL高温高压加氢微反装置进行, 评价原料采用大庆催 化裂化柴油, 该催化裂化柴油的比重 (df )为 0.8796, 硫含量为 890ppm, 总氮含量为
920ppm, 总芳烃含量为 55.2 v%。 原料采用柱塞泵泵入, 反应后的油样经高分离器冷却 后,在低分离器采集分析。加氢处理的温度为 400°C,压力为 6MPa,液时空速为 l.Oh—1, 氢油体积比为 800。 加氢处理后的催化剂评价结果如表 2所示。
表 1
Figure imgf000011_0001
表 2
催化剂 脱硫率, % 脱氮率, % 脱芳率, %
FZ-1 81.0 61.6 45.4
FZ-2 78.7 59.2 43.1
FZ-3 82.3 60.4 44.9
FZ-4 84.6 58.1 43.2 对比催化剂 1 93.9 72.3 58.8
对比催化剂 2 8.4 5.1 6.2 对比催化剂 3 65.2 55.1 40.1
实施例 10
本实施例提供实施例 1-7的催化剂对全熘分 FCC汽油进行加氢处理的应用。
实施例 1-7 的催化剂在应用前均进行了硫化处理, 使其具有加氢活性。 硫化采用 lOmL高温高压加氢微反装置进行, 其为湿法原位硫化, 即采用湿法硫化, 且硫化后催 化剂不卸出, 直接在反应器中继续进行加氢反应。硫化油为含 5wt% CS2的正癸垸溶液, 硫化的温度为 300°C, 时间为 6h,压力为 2MPa,液时空速为 lJh—1,氢油体积比为 300。
本实施例的加氢处理采用 10mL高温高压加氢微反装置进行, 评价原料采用全熘分
FCC汽油, 其比重 (d )为 0.7296, 硫含量为 470ppm, 研究法辛垸值(RON) 为 92.0。 原料采用柱塞泵泵入, 反应后的油样经高分离器冷却后, 在低分离器采集分析。 加氢处 理的温度为 280°C, 压力为 4MPa, 液时空速为 l.Oh—1, 氢油体积比为 300。 加氢处理后 的催化剂评价结果如表 3所示。
表 3
Figure imgf000012_0001
在上述实施例中, 催化剂的脱硫率、 脱氮率、 脱芳率、 油品的 RON以及汽油收率 的测定及计算方法均为本领域公知的测定及计算方法。
表 1、 表 2和表 3的结果说明: 相对于对比催化剂, 本发明的实施例提供的铁基加 氢催化剂具备较高的加氢脱硫、脱氮及脱芳活性。 而且, 本发明的铁基加氢催化剂用于 汽油加氢处理时, 能够使汽油的辛垸值损失很低。
本发明的实施例提供的铁基加氢催化剂的特征在于引入了更多的助活性组分元素, 并且相对于完全不引入助活性组分元素的对比催化剂 2来说, 引入锌的催化剂(对比催 化剂 3 ) 的加氢脱硫、 脱氮和脱芳率都有数倍至十倍的提升, 并且钾的引入可以进一步 促进只引入锌的催化剂 (对比催化剂 3 ) 的加氢脱硫活性。
虽然本发明的实施例提供的铁基加氢催化剂的脱硫、脱氮及脱芳率略低于传统负载 型 Ni-W催化剂 (对比催化剂 1 ) , 但本发明的实施例提供的铁基催化剂所采用的主活 性组分金属和助活性组分元素 (金属) 的价格远远低于传统加氢催化剂所采用的镍盐、 钴盐、钨盐和钼盐等。 并且, 本发明的实施例提供的铁基加氢催化剂突破了传统汽柴油 加氢催化剂沿用数十年的活性组分金属的限制, 具有长远的工业应用价值。
实施例 11
本实施例提供一种重油铁基加氢催化剂载体, 其制备方法包括以下步骤: 将 10g拟薄水铝石粉、 0.3g田菁粉混合均匀, 得到混合粉末;
将 0.3g稀硝酸、 0.3g柠檬酸溶于 20mL去离子水中, 得到混合溶液;
将混合溶液缓慢滴入到混合粉末中, 混合均匀形成可塑体, 在挤条机上挤出直径为 1.2mm的条状物;
再将条状物于 120°C的烘箱中烘干, 然后在 500°C、 空气气氛下焙烧 4小时, 得到 催化剂载体。
实施例 12
本实施例提供一种重油铁基加氢催化剂载体, 其制备方法包括以下步骤: 将 7g拟薄水铝石粉、 3gMCM-41分子筛、 0.3g田菁粉混合均匀, 得到混合粉末; 将 0.3g稀硝酸、 0.3g柠檬酸溶于 20mL去离子水中, 得到混合溶液;
将混合溶液缓慢滴入到所述混合粉末中, 混合均匀形成可塑体, 在挤条机上挤出直 径为 1.2mm的条状物;
再将条状物于 120°C的烘箱中烘干, 然后在 500°C、 空气气氛下焙烧 4小时, 得到 催化剂载体。
实施例 13
本实施例提供一种重油铁基加氢催化剂, 其制备方法包括以下步骤:
将 29.52g硝酸铁、 6.09g硝酸锌和 0.15g硝酸钾混合后溶于 20mL去离子水中, 配 成浸渍液;
将浸渍液缓慢滴加到 10g实施例 11的催化剂载体中混合均匀,得到催化剂半成品; 在室温下将催化剂半成品静置 4h, 然后于 120°C的烘箱中烘干, 再在 500°C、 空气 气氛下焙烧 4小时, 得到重油铁基加氢催化剂 Cl。
测得该重油铁基加氢催化剂 C1中铁锌钾氧化物的总量为 40%,其余为大孔氧化铝, 以该催化剂 C1的总重量为基准。 该重油铁基加氢催化剂 C1的比表面积、 孔体积和平 均孔径数据如表 5所示。其中, 催化剂比表面积、 孔体积和平均孔径的测定及计算方法 均为本领域公知的测定及计算方法。
实施例 14
本实施例提供一种重油铁基加氢催化剂, 其制备方法包括以下步骤: 将 25.30g硫酸铁、 12.18g氯化锌、 0.10g硫酸钾和 1.05g硝酸锆混合后溶于 20mL 去离子水中, 配成浸渍液;
将浸渍液缓慢滴加到 10g实施例 12的催化剂载体中混合均匀,得到催化剂半成品; 在室温下将催化剂半成品静置 4h, 然后于 120°C的烘箱中烘干, 再在 500°C、 空气 气氛下焙烧 4小时, 得到重油铁基加氢催化剂 C2。
测得该重油铁基加氢催化剂 C2中铁锌钾锆氧化物的总量为 40%, 其余为大孔氧化 铝和 MCM-41 , 以该催化剂 C2的总重量为基准。 该重油铁基加氢催化剂 C2的比表面 积、 孔体积和平均孔径的数据如表 5所示。
实施例 15
本实施例提供一种重油铁基加氢催化剂, 其制备方法包括以下步骤:
将 18.26g磷酸铁、 20.78g硫酸锌、 0.20g硝酸钾和 0.95g偏钒酸铵混合后溶于 20mL 去离子水中, 配成浸渍液;
将浸渍液缓慢滴加到 10g实施例 12的催化剂载体中混合均匀,得到催化剂半成品; 在室温下将催化剂半成品静置 8h, 然后于 120°C的烘箱中烘干, 再在 500°C、 空气 气氛下焙烧 6小时, 得到重油铁基加氢催化剂 C3。
测得该重油铁基加氢催化剂 C3中铁锌钾锆氧化物的总量为 40%, 其余为大孔氧化 铝和 MCM-41 , 以该催化剂 C3的总重量为基准。 该重油铁基加氢催化剂 C3的比表面 积、 孔体积和平均孔径的数据如表 5所示。
实施例 16
本实施例提供一种重油铁基加氢催化剂, 其制备方法包括以下步骤:
将 19.80g氯化铁、 14.18g硝酸锌、 0.32g硫酸钾和 l.OOg硫酸氧鈦混合均匀后, 在 120°C的烘箱中烘干, 再在 500°C、 空气气氛下焙烧 4小时, 得到重油铁基加氢催化剂 C4的氧化物粉末;
向该粉末中加入 0.5g去离子水,混合后放入压片机中压片成型, 即得到重油铁基加 氢催化剂 C4。
该重油铁基加氢催化剂 C4中铁锌钾鈦氧化物的总量为 100%, 以该催化剂 C4的总 重量为基准。 该重油铁基加氢催化剂 C4的比表面积、 孔体积和平均孔径的数据如表 5 所示。
实施例 17
本实施例提供一种重油铁基加氢催化剂, 其为采用共沉淀法制备得到的, 该制备方 法包括以下步骤: 将 32.44g氯化铁和 6.82g氯化锌溶于 250mL去离子水中, 得到氯化铁和氯化锌的 水溶液; 将 8g氢氧化钾溶于 80mL去离子水中, 得到氢氧化钾溶液; 边搅拌边将氢氧 化钾溶液缓慢加入到氯化铁和氯化锌的水溶液中;
在 80°C的水浴中搅拌反应 4小时,接着降温至 60°C静置老化 24小时,得到沉淀物; 将该沉淀物趁热过滤,用去离子水洗涤至 pH值约等于 9,然后于 120°C的烘箱中烘 干, 再以 5°C/min的速率升温, 在 500°C、 空气气氛下焙烧 2小时, 得到铁锌钾氧化物; 将 6.0g铁锌钾氧化物, 10g拟薄水铝石 (粘结剂), 0.4g田菁粉混合成均匀粉末, 得到混合粉末; 将 0.3g柠檬酸和 0.3g硝酸溶于 10mL去离子水中, 形成胶溶剂; 将该 胶溶剂加入该混合粉末并充分捏合, 在挤条机上挤成直径 1.5mm 的条状物, 将该条状 物在 120°C的烘箱中烘干, 然后在 500°C、 空气气氛下焙烧 8小时, 得到重油铁基加氢 催化剂 C5。
测得该催化剂 C5中铁锌钾氧化物的总量为 40%, 以该催化剂 C5的总重量为基准。 该重油铁基加氢催化剂 C5的比表面积、 孔体积和平均孔径的数据如表 5所示。
实施例 18
本实施例提供一种对比催化剂, 其制备方法包括以下步骤:
将 33.73g硝酸铁溶于 20mL去离子水中, 配成浸渍液;
将浸渍液缓慢滴加到 10g实施例 11的催化剂载体中混合均匀,得到催化剂半成品; 在室温下将催化剂半成品静置 4h, 然后于 120°C的烘箱中烘干, 再在 500°C、 空气 气氛下焙烧 4小时, 得到对比催化剂 C6。
测得该对比催化剂 C6中铁的氧化物的总量为 40%, 其余为大孔氧化铝, 以该催化 剂 C6的总重量为基准。该对比催化剂 C6的比表面积、孔体积和平均孔径的数据如表 5 所示。
实施例 19
本实施例提供一种对比催化剂, 其制备方法包括以下步骤:
将 27.62g硝酸铁和 6.78g硝酸锌溶于 20mL去离子水中, 配成浸渍液;
将浸渍液缓慢滴加到 10g实施例 12的催化剂载体中混合均匀,得到催化剂半成品; 在室温下将催化剂半成品静置 4h, 然后于 120°C的烘箱中烘干, 再在 500°C、 空气 气氛下焙烧 4小时, 得到对比催化剂 C7。
测得该对比催化剂 C7中铁锌氧化物的总量为 40%,其余为大孔氧化铝和 MCM-41, 以该催化剂 C7的总重量为基准。 该对比催化剂 C7的比表面积、 孔体积和平均孔径的 数据如表 5所示。 实施例 20
本实施例提供一种对比催化剂, 其制备方法包括以下步骤:
将 2.27g偏钨酸铵和 2.43g硝酸镍溶于 20mL去离子水中, 配成浸渍液;
将浸渍液缓慢滴加到 10g实施例 12的催化剂载体中混合均匀,得到催化剂半成品; 在室温下将催化剂半成品静置 4h, 然后于 120°C的烘箱中烘干, 再在 500°C、 空气 气氛下焙烧 4小时, 得到重油加氢催化剂 C8。
测得该对比催化剂 C8中钨镍氧化物的总量为 20%,其余为大孔氧化铝和 MCM-41, 以该催化剂 C8的总重量为基准。 该对比催化剂 C8的比表面积、 孔体积和平均孔径的 数据如表 5所示。
实施例 21
本实施例提供实施例 13-20的催化剂对常压渣油进行加氢处理的应用。
实施例 13-20的催化剂在应用前均进行了硫化处理, 使其具有加氢活性。 硫化采用 50mL高温高压加氢微反装置进行, 其为湿法原位硫化, 即采用湿法硫化, 且硫化后催 化剂不卸出, 直接在反应器中继续进行加氢反应。硫化油为含 5wt% CS2的正癸垸溶液, 硫化的温度为 300°C,时间为 10h,压力为 4MPa,液时空速为 Ι^ΙιΛ氢油体积比为 300。
本实施例的加氢处理采用 50mL高温高压加氢微反装置进行, 评价原料采用沙中常 压渣油(其性质如表 4所示)。 原料采用柱塞泵泵入, 反应后的油样经高分离器冷却后, 在低分离器采集分析。 加氢处理的温度为 400°C, 压力为 10MPa, 液时空速为 l.Oh—1, 氢油体积比为 1000。 加氢处理后的催化剂评价结果如表 5所示。
表 4
Figure imgf000016_0001
表 5
催化剂 C1 C2 C3 C4 C5 C6 C7 C8 比表面积, m2/g 170 315 325 71 102 324 173 357 孔体积, cc/g 0.77 0.98 0.92 0.32 0.67 0.93 0.76 1.01 平均孔径, nm 11.9 9.0 11.4 8.0 8.2 9.4 12.3 11.1 脱硫率, % 50.4 54.1 55.0 55.2 49.8 7.9 47.1 67.0 脱氮率, % 31.8 32.9 34.1 33.8 31.0 5.1 30.5 40.2 实施例 22
本实施例提供实施例 15、 实施例 16、 实施例 19和实施例 20的催化剂对焦化蜡油 进行加氢处理的应用。
实施例 15、 16、 19、 20的催化剂在应用前均进行了硫化处理, 使催化剂具有更好 的加氢效果。 硫化采用 50mL高温高压加氢微反装置进行, 其为湿法原位硫化, 即采用 湿法硫化, 且硫化后催化剂不卸出, 直接在反应器中继续进行加氢反应。 硫化油为含 5wt% CS2的正癸垸溶液, 硫化的温度为 400°C, 时间为 8h, 压力为 5MPa, 液时空速为 1.511-1 , 氢油体积比为 300。
本实施例的加氢处理采用 50mL高温高压加氢微反装置进行, 评价原料采用大港焦 化蜡油, 硫含量为 0.253wt%, 总氮含量为 0.51wt%。原料采用柱塞泵泵入, 反应后的油 样经高分离器冷却后, 在低分离器采集分析。 加氢处理的温度为 360°C, 压力为 6MPa, 液时空速为 l h—1, 氢油体积比为 500。
加氢处理后的催化剂评价结果如表 6所示。
表 6
Figure imgf000017_0001
实施例 23
本实施例提供实施例 15、 实施例 16、 实施例 19和实施例 20的催化剂对减压渣油 进行加氢处理的应用。
实施例 15、 16、 19、 20的催化剂在应用前均进行了硫化处理, 使催化剂具有更好 的加氢效果。 硫化采用 50mL高温高压加氢微反装置进行, 其为湿法原位硫化, 即采用 湿法硫化, 且硫化后催化剂不卸出, 直接在反应器中继续进行加氢反应。 硫化油为含 5wt% CS2的正癸垸溶液, 硫化的温度为 360°C, 时间为 12h, 压力为 4MPa, 液时空速 为 21^, 氢油体积比为 300。
本实施例的加氢处理采用 50mL高温高压加氢微反装置进行, 评价原料采用沙中减 压渣油(其性质如表 7所示)。原料采用柱塞泵泵入, 反应后的油样经高分离器冷却后, 在低分离器采集分析。加氢处理的温度为 360°C, 压力为 8MPa, 液时空速为 lh—1, 氢油 体积比为 800。
加氢处理后的催化剂评价结果如表 8所示。 表 7
Figure imgf000018_0001
表 8
Figure imgf000018_0002
表 5、 表 6和表 8的结果说明本发明的实施例的重油铁基加氢催化剂具有很高的重 油加氢脱硫、脱氮以及脱金属活性。本发明的实施例的铁基加氢催化剂的特征在于引入 了助活性组分元素(金属) , 并且相对于完全不引入助活性组分元素(金属) 的对比催 化剂 C6来说, 引入锌的催化剂(对比催化剂 C7)的加氢脱硫率有数倍的提升, 并且钾 的引入可以进一步促进只引入锌的催化剂 (对比催化剂 C7) 的加氢脱硫活性。
虽然本发明的实施例的催化剂的脱硫、 脱氮率和金属脱除率略低于传统负载型 Ni-W催化剂(对比催化剂 C8) , 但本发明的实施例的催化剂所采用的活性组分金属和 助金属的价格远远低于传统加氢催化剂所采用的镍盐、 钴盐、 钨盐和钼盐等。 并且, 本 发明的实施例的铁基加氢催化剂突破了传统加氢催化剂沿用数十年的活性组分金属的 限制, 具有重要的理论研究价值和工业应用价值。

Claims

权利要求书
1、 一种铁基加氢催化剂, 该铁基加氢催化剂以铁作为主活性组分金属, 以锌和钾 为第一助活性组分金属;
以该铁基加氢催化剂的总重量为基准,所述主活性组分金属和助活性组分元素的总 量为 5-100%, 余量为粘结剂或载体, 以氧化物形式计; 所述助活性组分元素包括第一 助活性组分金属;
其中, 所述主活性组分金属和所述第一助活性组分金属的摩尔比为 0.5-200: 1。
2、 根据权利要求 1所述的铁基加氢催化剂, 其中, 所述主活性组分金属和所述第 一助活性组分金属的摩尔比为 0.8-20: 1。
3、 根据权利要求 1所述的铁基加氢催化剂, 其中, 以该铁基加氢催化剂的总重量 为基准, 所述主活性组分金属和助活性组分元素的总量为 20-70%, 余量为粘结剂或载 体, 以氧化物形式计; 所述助活性组分元素包括第一助活性组分金属。
4、 根据权利要求 3所述的铁基加氢催化剂, 其中, 以该铁基加氢催化剂的总重量 为基准, 所述主活性组分金属和助活性组分元素的总量为 20-50%, 余量为粘结剂或载 体, 以氧化物形式计, 所述助活性组分元素包括第一助活性组分金属。
5、 根据权利要求 1所述的铁基加氢催化剂, 其中, 该铁基加氢催化剂还包括选自 IVB、 VA、 VB、 VIB和 VIII族元素的第二助活性组分元素;
其中, 所述主活性组分金属与所述第二助活性组分元素的摩尔比为 0.5-200: 1; 以该铁基加氢催化剂的总重量为基准,主活性组分金属和助活性组分元素的总量为 5-100%, 余量为粘结剂或载体, 以氧化物形式计;
所述助活性组分元素包括第一助活性组分金属和第二助活性组分元素。
6、 根据权利要求 5所述的铁基加氢催化剂, 其中, 所述主活性组分金属与所述第 二助活性组分元素的摩尔比为 5-100: 1。
7、 根据权利要求 5所述的铁基加氢催化剂, 其中, 所述 IVB元素包括鈦、 锆, 所 述 VA元素包括磷,所述 VB元素包括钒,所述 VIB元素包括铬,所述 VIII族元素包括 钴、 镍、 钯和铂。
8、 根据权利要求 5所述的铁基加氢催化剂, 其中, 以该铁基加氢催化剂的总重量 为基准, 所述主活性组分金属和助活性组分元素的总量为 20-50%, 余量为粘结剂或载 体, 以氧化物形式计; 所述助活性组分元素包括第一助活性组分金属与第二助活性组分 元素。
9、 根据权利要求 1或 5所述的铁基加氢催化剂, 其是由浸渍法、 共沉淀法或压片 法制备得到的。
10、 根据权利要求 9所述的铁基加氢催化剂, 其中, 所述浸渍法包括以下步骤: 将主活性组分金属的盐、 第一助活性组分金属的盐溶于去离子水中, 配成浸渍液; 将所述浸渍液加入到载体中, 得到催化剂半成品;
将所述催化剂半成品在空气中静置 2-24小时, 然后烘干, 再在空气气氛、 200-800 °C焙烧 2-8h, 得到所述铁基加氢催化剂。
11、 根据权利要求 10所述的铁基加氢催化剂, 其中, 所述第二助活性组分元素的 盐与主活性组分金属的盐、 第一助活性组分金属的盐一起溶于去离子水中。
12、 根据权利要求 10所述的铁基加氢催化剂, 其中, 所述载体包括黄铁矿、 磁黄 铁矿、 三氧化二铁、 四氧化三铁、 氧化铝、 二氧化硅、 无定形硅铝和沸石分子筛中的一 种或几种的组合。
13、 根据权利要求 9所述的铁基加氢催化剂, 其中, 所述共沉淀法包括以下步骤: 将主活性组分金属的盐和第一助活性组分元素的盐的水溶液以及沉淀剂的水溶液 混合均匀;
然后在 40-95Ό水浴中搅拌反应 l-24h, 再在 40-95 °C水浴中静置老化 2-48h, 得到 沉淀物;
将所述沉淀物进行过滤、 水洗、 烘干后, 得到催化剂前驱体;
将所述催化剂前驱体在空气气氛、 200-800°C焙烧 2-8h, 得到金属氧化物; 将所述金属氧化物与粘结剂混合进行成型处理, 得到所述铁基加氢催化剂。
14、 根据权利要求 13所述的铁基加氢催化剂, 其中, 所述第二助活性组分元素的 盐与主活性组分金属的盐、 第一助活性组分金属的盐一起与沉淀剂的水溶液混合。
15、 根据权利要求 13所述的铁基加氢催化剂, 其中, 所述粘结剂包括氧化铝、 硅 溶胶、 铝溶胶和水玻璃中的一种或几种的组合。
16、根据权利要求 13所述的铁基加氢催化剂,其中,所述沉淀剂包括 NaOH、 KOH、 Na2C03, K2C03、 Na2S、 (NH4)2S, 尿素和氨水中的一种或几种的组合, 所述沉淀剂与 所述主活性组分金属、所述第一助活性组分金属、所述第二助活性组分元素的摩尔比为 1-6: 1。
17、根据权利要求 10或 13所述的铁基加氢催化剂, 其中, 所述主活性组分金属的 盐包括硝酸铁、硫酸铁、 氯化铁和磷酸铁中的一种或几种的组合; 所述第一助活性组分 金属的盐包括硝酸盐、 硫酸盐、 氯化盐和磷酸盐中的一种或几种的组合。
18、根据权利要求 9所述的铁基加氢催化剂,其中,所述压片成型法包括以下步骤: 将主活性组分金属的盐和第一助活性组分元素的盐混合均匀;
将主活性组分金属的盐、 第一助活性组分金属的盐混合均匀, 然后烘干, 再在空气 气氛、 200-800°C焙烧 2-8h, 得到所述铁基加氢催化剂的氧化物粉末;
向所述的铁基加氢催化剂的氧化物粉末中加入少量水, 放入压片机中压片成型, 得 到所述铁基加氢催化剂。
19、 根据权利要求 18所述的铁基加氢催化剂, 其中, 所述第二助活性组分元素的 盐与主活性组分金属的盐、 第一助活性组分金属的盐一起混合均匀。
20、 根据权利要求 11、 14或 19所述的铁基加氢催化剂, 其中, 所述第二助活性组 分元素的盐包括硝酸盐、 硫酸盐、 氯化盐和磷酸盐中的一种或几种的组合。
21、 权利要求 1所述的铁基加氢催化剂在直熘汽油、 直熘柴油、 焦化汽油、 焦化柴 油、 催化裂化汽油、 催化裂化柴油以及常压渣油、 减压渣油、 煤焦油、 脱沥青油以及从 油砂或页岩中提取的重质油中的一种或几种的混合油的加氢处理中的应用。
22、 根据权利要求 21所述的应用, 其中, 所述铁基加氢催化剂为经过硫化处理的 铁基加氢催化剂, 所述硫化处理的温度为 200-450°C, 压力为 0.1-10MPa, 硫化处理的 时间为 2-48小时, 液时空速为 0.1-2011-1, 氢油体积比为 100-800。
23、 根据权利要求 22所述的应用, 其中, 所述硫化处理的温度为 280-380°C, 压力 为 2-6MPa,预硫化处理的时间为 6-24小时,液时空速为 Ι^ΙιΛ氢油体积比为 200-500。
24、 根据权利要求 21所述的应用, 其中, 所述加氢处理的温度为 200-600°C, 压力 为 l-20MPa, 液时空速为 Ο.Ι-lOh·1, 氢油体积比为 100-2000。
25、 根据权利要求 22所述的应用, 其中, 所述加氢处理的温度为 250-400°C, 压力 为 2-10MPa, 液时空速为 Ο^-δΙι·1, 氢油体积比为 200-1000。
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