CN105289720A - Hydrocarbon oil desulfurization catalyst and preparation method thereof, and hydrocarbon oil desulfurization method - Google Patents
Hydrocarbon oil desulfurization catalyst and preparation method thereof, and hydrocarbon oil desulfurization method Download PDFInfo
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Abstract
The invention discloses a hydrocarbon oil desulfurization catalyst and a preparation method thereof, and a hydrocarbon oil desulfurization method. Based on the total weight of the hydrocarbon oil desulfurization catalyst as the reference, the hydrocarbon oil desulfurization catalyst comprises 10-80 wt% of at least one of metal oxides of IIB, VB, and VIB group elements, 3-35 wt% of aluminium oxide, 5-40 wt% of silicon nitride, 5-30 wt% of a metal accelerant selected from at least one of cobalt, nickel, iron and manganese, and 1-20 wt% of an SAPO molecular sieve. The hydrocarbon oil desulfurization catalyst is excellent in stability, higher in desulfurization activity, better in wear resistance and longer in service life.
Description
Technical field
The present invention relates to a kind of method of desulfurization of hydrocarbon oil Catalysts and its preparation method and desulfurization of hydrocarbon oil, particularly, relate to a kind of desulfurization of hydrocarbon oil catalyst, the method preparing desulfurization of hydrocarbon oil catalyst and the desulfurization of hydrocarbon oil catalyst obtained by the method, and use this desulfurization of hydrocarbon oil catalyst to carry out the method for desulfurization of hydrocarbon oil.
Background technology
Along with people are to the pay attention to day by day of environmental protection, environmental regulation is also day by day strict, and the sulfur content reducing gasoline and diesel oil is considered to one of most important measure improving air quality.Most of sulphur in China's gasoline products come from hot-working petroleum blending component, as catalytically cracked gasoline.Therefore in hot-working petroleum, the minimizing of sulfur content contributes to the sulfur content reducing China's gasoline products.The existing gasoline products standard GB17930-2011 " motor petrol " of China required on December 31st, 2013, and in gasoline products, sulfur content must drop to 50 μ g/g.And the gasoline product quality standard in future will be stricter.In this case, catalytically cracked gasoline has to pass through deep desulfuration gasoline products just can be made to meet the requirement of environmental protection.
At present, the process for deep desulphurization of oil product mainly contains selective catalytic hydrogenation desulfurization and catalytic hydrogenation adsorption desulfurize two kinds of methods.Catalytic hydrogenation adsorption desulfurize be certain temperature, pressure and face hydrogen condition under realize the sulfur compounds adsorption in hydrocarbon ils to remove, this technology has low and not high to the purity requirement of the hydrogen feature of hydrogen consumption, and this technology is had broad application prospects in fuel desulfuration.
CN1355727A discloses a kind of adsorbent composition being applicable to remove sulphur from cracking gasoline and diesel fuel, be made up of zinc oxide, silica, oxidation al and ni, wherein nickel is substantially to reduce valence state existence, and its amount can remove sulphur from the cracking gasoline contacted with described nickeliferous adsorbent composition under desulfurization conditions or diesel fuel stream.Said composition forms particle by compound particles granulation zinc oxide, silica and aluminium oxide formed, and with nickel or nickel compound containing dipping after dry, roasting, then drying, roasting, reduction obtain.
CN1382071A discloses a kind of adsorbent composition being applicable to remove sulphur from cracking gasoline and diesel fuel, be made up of zinc oxide, silica, aluminium oxide and cobalt, wherein cobalt exists substantially to reduce valence state, and its amount can from removing sulphur under desulfurization conditions with the described cracking gasoline that contacts containing cobalt adsorbent composition or diesel fuel stream.
US6150300 discloses a kind of method preparing adsorbent, comprises and prepares spheric granules: silica containing composition, the composition containing dispersion metal oxide in an aqueous medium and the composition containing zinc oxide are mixed to form the first mixture and do not extrude described first mixture by (a); B described first mixture globulate is formed the particle with diameter 10-1000mm by ().Wherein step (a) also comprises and mixing with metallic promoter agent.
CN1422177A discloses a kind of adsorbent composition being applicable to remove sulphur from cracking gasoline and diesel fuel, be made up of zinc oxide, expanded perlite, aluminium oxide and promoter metals, wherein said promoter metals exists with the amount that can remove sulphur when contacting with it under desulfurization conditions from cracking gasoline or diesel fuel stream with the valence state substantially reduced.
CN1627988A discloses a kind of adsorbent composition being suitable for removing elementary sulfur and sulphur compound from cracking gasoline and diesel fuel, described adsorbent composition comprises: zinc oxide, expanded perlite, aluminate and promoter metals, wherein said promoter metals is will cause the amount of desulfurization from the stream of cracking gasoline or diesel fuel to exist when making cracking gasoline or diesel fuel stream contacts under desulfurization conditions with it, and at least part of described promoter metals exists with 0 valence state.
CN1856359A discloses a kind of method of production combination thing, comprising: a) mixing material, zinc compound, containing earth silicon material, aluminium oxide and co-catalyst, to form its mixture; B) this mixture dry, to form the mixture of drying; C) mixture of this drying is calcined, to form the mixture through calcining; D) under suitable condition this mixture through calcining is reduced with suitable reducing agent, to produce in it composition of the co-catalyst content with reduction valence state, and e) reclaim reorganization compound.Co-catalyst contains various metals such as being selected from nickel.
CN1871063A discloses a kind of method of production combination thing, and the method comprises: a) by liquid, zinc compound, containing earth silicon material, aluminium oxide mixing to form its mixture; B) by this mixing dry for described mixture to form the first drying mixture; C) described first drying mixture is calcined to form first through calcining mixt; D) promoter is attached to described first within calcining mixt or on formed through promote mixture; E) make described through promote mixture and be selected from citric acid, the acid of tartaric acid and combination thereof contacts to be formed through contact mixture; F) by described dry to form the second drying mixture through contact mixture; G) described second drying mixture is calcined to form second through calcining mixt; H) adopt applicable reducing agent reduction described second under suitable condition through calcining mixt to produce the composition wherein containing reduction valence state promoter content, and i) reclaim described composition.
Although published adsorbent has certain desulfurization performance, along with the raising of gasoline quality standard, product gasoline sulfur content is required also constantly strict.And this type of catalyst in use easily weares and teares, need continuous make-up catalyst, improve operating cost.As can be seen here, need to provide a kind of new catalyst with more high desulfurization activity and abrasion resistance properties.
Summary of the invention
The object of the invention is the defect of desulphurizing activated low, the structural instability of adsorbent in order to overcome prior art and abrasion resistance properties difference, providing a kind of method of desulfurization of hydrocarbon oil Catalysts and its preparation method and desulfurization of hydrocarbon oil.
To achieve these goals, the invention provides a kind of desulfurization of hydrocarbon oil catalyst, with the gross weight of this desulfurization of hydrocarbon oil catalyst for benchmark, this desulfurization of hydrocarbon oil catalyst contains: 1) at least one of 10-80 % by weight is selected from the metal oxide of IIB, VB and group vib element; 2) aluminium oxide of 3-35 % by weight; 3) silicon nitride of 5-40 % by weight; 4) metallic promoter agent of 5-30 % by weight, described metallic promoter agent is selected from least one in cobalt, nickel, iron and manganese; 5) the SAPO molecular sieve of 1-20 % by weight.
Present invention also offers the preparation method of desulfurization of hydrocarbon oil catalyst of the present invention, the method comprises: silicon nitride, alumina binder, at least one are selected from the metal oxide of IIB, VB and group vib element, SAPO molecular sieve, water and acidic liquid mixing by (1), and the carrier pulp be mixed to get is carried out shaping, first dry, the first roasting, obtain carrier; (2) in described carrier, introduce the precursor of metallic promoter agent, then carry out second dry and the second roasting, obtain catalyst precarsor; (3) described catalyst precarsor is reduced in a hydrogen atmosphere, obtain desulfurization of hydrocarbon oil catalyst.
Present invention also offers the desulfurization of hydrocarbon oil catalyst that preparation method provided by the invention obtains.
The invention provides a kind of method of desulfurization of hydrocarbon oil, the method comprises: in a hydrogen atmosphere, and by hydrocarbon oil containing surphur and desulfurization of hydrocarbon oil catalyst exposure provided by the invention, the temperature of described contact is 350-500 DEG C, and the pressure of described contact is 0.5-4MPa.
Containing stable silicon nitride in the composition of desulfurization of hydrocarbon oil catalyst provided by the invention, decrease the dependent interaction with metal oxides such as zinc oxide, avoid the formation of zinc silicate material, in such as, XRD spectra after the hydrothermal aging of the desulfurization of hydrocarbon oil catalyst A 1 of embodiment 1 acquisition of Fig. 1 display, there is not the characteristic peak of zinc silicate.Desulfurization of hydrocarbon oil catalyst provided by the invention has the desulphurizing activated of better stability and Geng Gao, more effectively can be adsorbed onto on desulfurization of hydrocarbon oil catalyst by the sulphur in hydrocarbon ils, obtain the hydrocarbon ils that sulfur content is lower in desulfurization of hydrocarbon oil process.And desulfurization of hydrocarbon oil catalyst provided by the invention has better abrasion resistance properties, and in sweetening process, catalyst attrition is lower, longer service life.
Other features and advantages of the present invention are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the XRD collection of illustrative plates of desulfurization of hydrocarbon oil catalyst A 1 before and after hydrothermal aging that embodiment 1 obtains;
Fig. 2 is the XRD collection of illustrative plates of desulfurization of hydrocarbon oil catalyst B 1 before and after hydrothermal aging that comparative example 1 obtains.
Detailed description of the invention
Below the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The invention provides a kind of desulfurization of hydrocarbon oil catalyst, with the gross weight of this desulfurization of hydrocarbon oil catalyst for benchmark, this desulfurization of hydrocarbon oil catalyst contains: 1) at least one of 10-80 % by weight is selected from the metal oxide of IIB, VB and group vib element; 2) aluminium oxide of 3-35 % by weight; 3) silicon nitride of 5-40 % by weight; 4) metallic promoter agent of 5-30 % by weight, described metallic promoter agent is selected from least one in cobalt, nickel, iron and manganese; 5) the SAPO molecular sieve of 1-20 % by weight.
Preferably, the content of described metal oxide is 25-70 % by weight, and the content of described aluminium oxide is 6-25 % by weight, and the content of silicon nitride is 10-30 % by weight, the content of described metallic promoter agent is 8-25 % by weight, and the content of described SAPO molecular sieve is 1-10 % by weight.
More preferably, the content of described metal oxide is 40-60 % by weight, and the content of described aluminium oxide is 8-15 % by weight, and the content of silicon nitride is 12-25 % by weight, the content of described metallic promoter agent is 12-20 % by weight, and the content of described SAPO molecular sieve is 2-10 % by weight.
According to the present invention, silicon nitride is white powder, and silicon nitride can be α phase silicon nitride and/or beta phase silicon nitride, and under preferable case, silicon nitride is α phase silicon nitride.The particle diameter of alpha-silicon nitride powders can be preferably (i.e. 6.5-25 μm) between 2000-500 order.
Desulfurization of hydrocarbon oil catalyst provided by the invention contains silicon nitride, can effectively avoid forming zinc silicate in the composition carrying out this catalyst in desulfurization of hydrocarbon oil process, ensures that this catalyst has better desulphurizing activated.Preferably, be the characteristic peak that 22.0,25.54,48.9 and 59.4 places do not have zinc silicate at 2 θ in the XRD spectra of described desulfurization of hydrocarbon oil catalyst after hydrothermal aging.Described hydrothermal aging is temperature 500-700 DEG C, steam partial pressure is 10-30kPa, and the processing time is 10-24h.
According to the present invention, described SAPO molecular sieve is nearly body silicoaluminophosphate, is introduced by silicon in aluminum phosphate skeleton and obtains, and its skeleton is by PO
4 +, AlO
4 -and SiO
2tetrahedron forms.This molecular sieve analog comprises 13 kinds of three-dimensional microporous framework structures, and its hole size is
pore volume is 0.18-0.48cm
3/ g.Under preferable case, described SAPO molecular sieve is at least one in SAPO-5, SAPO-11, SAPO-31, SAPO-34 and SAPO-20.The hole size of SAPO-5, SAPO-11, SAPO-31, SAPO-34 and SAPO-20 molecular sieve is respectively
(12 ring),
(10 ring),
(10 ring),
(8 ring) and
(6 ring); Pore volume is respectively 0.31,0.18,0.42,0.42 and 0.40cm
3/ g.Preferably, described SAPO molecular sieve is at least one in SAPO-11, SAPO-31 and SAPO-34.
According to the present invention, described at least one is selected from the metal oxide of IIB, VB and group vib element can at least one in zinc oxide, cadmium oxide, vanadium oxide, niobium oxide tantalum oxide, chromium oxide, molybdenum oxide and tungsten oxide, under preferable case, described metal oxide is at least one in zinc oxide, molybdenum oxide and vanadium oxide; Preferably, described metal oxide is zinc oxide.
According to the present invention, preferably, described metallic promoter agent is nickel and/or cobalt, and described desulfurization of hydrocarbon oil catalyst has higher desulphurizing activated and regenerability; More preferably, described metallic promoter agent is nickel.
In the present invention, described aluminium oxide can for providing cementation between each component in described desulfurization of hydrocarbon oil catalyst.Under preferable case, described aluminium oxide is at least one in gama-alumina, η-aluminium oxide, θ-aluminium oxide and χ-aluminium oxide; Preferably, described aluminium oxide is gama-alumina.
Present invention also offers the preparation method of desulfurization of hydrocarbon oil catalyst of the present invention, the method comprises: silicon nitride, alumina binder, at least one are selected from the metal oxide of IIB, VB and group vib element, SAPO molecular sieve, water and acidic liquid mixing by (1), and the carrier pulp be mixed to get is carried out shaping, first dry, the first roasting, obtain carrier; (2) in described carrier, introduce the precursor of metallic promoter agent, then carry out second dry and the second roasting, obtain catalyst precarsor; (3) described catalyst precarsor is reduced in a hydrogen atmosphere, obtain desulfurization of hydrocarbon oil catalyst.
The process of preparation method's step (1) the described mixing of desulfurization of hydrocarbon oil catalyst provided by the invention can to the opportunity that adds of silicon nitride, there is no particular limitation, and a kind of detailed description of the invention is: the process of step (1) described mixing comprises: the contact of silicon nitride, alumina binder, water and acidic liquid is formed slurries by (i): described slurries and SAPO molecular sieve, described metal oxide are mixed to get carrier pulp by (ii).
Another kind of detailed description of the invention is: the process of step (1) described mixing comprises: alumina binder, water and acidic liquid contact and form slurries by (a): described slurries and SAPO molecular sieve, described metal oxide, silicon nitride are mixed to get carrier pulp by (b).
In preparation method's step (1) of desulfurization of hydrocarbon oil catalyst provided by the invention, described metal oxide for add with the powder type of described metal oxide, also can add water after being mixed into slurries and add in form of slurry by adding of described metal oxide.
According to the present invention, described alumina binder for aluminium oxide or can change γ-Al under the condition of described first roasting
2o
3material.Under preferable case, in step (1), described alumina binder can be selected from least one in SB powder, hydrated alumina, Alumina gel, boehmite (boehmite), false boehmite (boehmite), hibbsite and amorphous hydroted alumina; Preferably, described alumina binder is at least one in SB powder, boehmite and Alumina gel.
In the present invention, it is described above that described at least one is selected from the metal oxide of IIB, VB and group vib element, SAPO molecular sieve, metallic promoter agent and silicon nitride, and this is no longer going to repeat them.
According to the present invention, described acidic liquid can be acid or aqueous acid, and described acid can be selected from water-soluble inorganic acid and/or organic acid, and preferably described acid can be at least one in hydrochloric acid, nitric acid, phosphoric acid and acetic acid.
According to the present invention, in step (i) and (a), under preferable case, the consumption of described acidic liquid makes the pH value of described slurries be 1-5, and preferable ph is 1.5-4.
In the present invention, the amount adding water in step (i) and (a) can not limit, especially as long as can obtain described slurries.Such as add the amount of water and alumina binder or be 5-10:1 with the weight ratio of the weight summation of alumina binder and silicon nitride.
In the present invention, the carrier pulp that step (1) obtains can be the form such as pastel or slurries.Can by dry reshaping after this carrier pulp multiviscosisty.More preferably this carrier pulp is slurry form, can form the microballoon that granularity is 20-200 micron, reach shaping object by spraying dry.For the ease of spraying dry, before dry, the solid content of described carrier pulp can be 10-50 % by weight, is preferably 20-50 % by weight.Obtain can also comprising in the process of described carrier pulp adding water in step (ii) and (b), there is no particular limitation for the addition of water, as long as the carrier pulp obtained meets above-mentioned solid content.
In the present invention, the first drying means of carrier pulp and condition are conventionally known to one of skill in the art in step (1), such as dry method can be dry, dry, forced air drying.Under preferable case, the temperature of described first drying can be room temperature to 400 DEG C, is preferably 100-350 DEG C; The time of described first roasting is more than 0.5h, is preferably 0.5-100h, more preferably 2-20h.
In the present invention, in step (1), the first roasting condition of carrier pulp is also conventionally known to one of skill in the art, and under preferable case, the temperature of described first roasting is 400-700 DEG C, is preferably 450-650 DEG C; The time of described first roasting is at least 0.5h, is preferably 0.5-100h, is more preferably 0.5-10h.
According to the present invention, step (2) is for adding metallic promoter agent.The precursor of described metallic promoter agent is the material that can change the oxide of metallic promoter agent under the second roasting condition into; Under preferable case, the precursor of described metallic promoter agent can be selected from least one in the acetate of metallic promoter agent, carbonate, nitrate, sulfate, rhodanate and oxide.
According to the present invention, under preferable case, carrier is introduced the method for the precursor of metallic promoter agent for dipping or precipitation.Described dipping can be the solution of the precursor by metallic promoter agent or suspension impregnation carrier; Described precipitation can be the solution of the precursor of metallic promoter agent or suspension are mixed with carrier, then adds ammoniacal liquor by the precursor precipitation of metallic promoter agent on carrier.
According to the present invention, under preferable case, the temperature of described second drying is 50-300 DEG C, and the time of described second drying is 0.5-8h; Preferably, the temperature of described second drying is 100-250 DEG C, and the time of described second drying is 1-5h; The temperature of described second roasting is 300-800 DEG C, and the time of described second roasting is more than 0.5h; Preferably, the temperature of described second roasting is 450-750 DEG C, and the time of described second roasting is 1-3h.Described second roasting can be carried out under having oxygen or oxygen-containing gas to exist, until volatile materials is removed and the precursor of metallic promoter agent is converted into the oxide form of metallic promoter agent, obtains catalyst precarsor.
According to the present invention, in step (3), change the oxide of the metallic promoter agent in described catalyst precarsor into metal simple-substance, described catalyst precarsor can be reduced under hydrogen atmosphere, metallic promoter agent is existed with reduction-state substantially, obtains catalyst of the present invention.The condition of described reduction only changes the oxide of the metallic promoter agent in described catalyst precarsor into metal simple-substance, and the metal oxide in described carrier can not change.Under preferable case, the temperature of described reduction is 300-600 DEG C, and the time of described reduction is 0.5-6h, and in described hydrogen atmosphere, the content of hydrogen is 10-60 volume %; The temperature of preferred described reduction is 400 DEG C-500 DEG C, and the time of preferred described reduction is 1-3h.
In the present invention, catalyst precarsor reduction can be carried out immediately by step (3) after obtained catalyst precarsor, also can before use (namely for desulfurization absorption before) carry out.Because metallic promoter agent is easily oxidized, and the metallic promoter agent in catalyst precarsor exists in the form of an oxide, and therefore for ease of transport, catalyst precarsor reduction is carried out by preferred steps (3) before carrying out desulfurization absorption.Described being reduced to makes the metal in the oxide of metallic promoter agent substantially exist with reduction-state, obtains desulphurization catalyst of the present invention.
According to the present invention, under preferable case, the addition of the precursor of silicon nitride, described alumina binder, described metal oxide, described SAPO molecular sieve and described metallic promoter agent makes in the desulfurization of hydrocarbon oil catalyst obtained, with the gross weight of described desulfurization of hydrocarbon oil catalyst for benchmark, the described SAPO molecular sieve of the described metal oxide containing 10-80 % by weight, the aluminium oxide of 3-35 % by weight, the silicon nitride of 5-40 % by weight, the described metallic promoter agent of 5-30 % by weight and 1-20 % by weight; Preferably, the described SAPO molecular sieve of the described metal oxide containing 25-70 % by weight, the aluminium oxide of 6-25 % by weight, the silicon nitride of 10-30 % by weight, the described metallic promoter agent of 8-25 % by weight and 1-10 % by weight; More preferably, the described SAPO molecular sieve of the described metal oxide containing 40-60 % by weight, the aluminium oxide of 8-15 % by weight, the silicon nitride of 12-25 % by weight, the described metallic promoter agent of 12-20 % by weight and 2-10 % by weight.
Present invention also offers the desulfurization of hydrocarbon oil catalyst obtained by preparation method provided by the invention.
The invention provides a kind of method of desulfurization of hydrocarbon oil, the method comprises: in a hydrogen atmosphere, and by hydrocarbon oil containing surphur and desulfurization of hydrocarbon oil catalyst exposure provided by the invention, the temperature of described contact is 350-500 DEG C, and the pressure of described contact is 0.5-4MPa; Preferably, the temperature of described contact is 400-450 DEG C, and the pressure of described contact is 1.0-2.0MPa.Sulphur in the process in hydrocarbon ils is adsorbed on catalyst, thus obtains the hydrocarbon ils of low sulfur content.
In the present invention, reacted catalyst can be reused after regeneration.Described regeneration is carried out under oxygen atmosphere, and the condition of regeneration comprises: the pressure of regeneration is normal pressure, and the temperature of regeneration is 400-700 DEG C, is preferably 500-600 DEG C.
In the present invention, the catalyst after regeneration is before re-starting desulfurization of hydrocarbon oil, and also need to reduce under hydrogen atmosphere, the reducing condition of the catalyst after regeneration comprises: temperature is 350-500 DEG C, is preferably 400-450 DEG C; Pressure is 0.2-2MPa, is preferably 0.2-1.5MPa.
In the present invention, described hydrocarbon ils comprises cracking gasoline and diesel fuel, and wherein " cracking gasoline " means hydrocarbon or its any cut that boiling range is 40 DEG C to 210 DEG C, is the product from making larger crack hydrocarbon molecules become more micromolecular heat or catalytic process.The thermal cracking process be suitable for includes, but are not limited to coking, thermal cracking and visbreaking etc. and combination thereof.The example of the catalytic cracking process be suitable for includes but not limited to fluid catalystic cracking and RFCC etc. and combination thereof.Therefore, the catalytically cracked gasoline be suitable for includes but not limited to coker gasoline, pressure gasoline, visbreaker gasoil, fluid catalystic cracking gasoline and heavy oil cracked gasoline and combination thereof.In some cases, be in the methods of the invention used as hydrocarbon-containifluids fluids time can by described cracking gasoline fractionation and/or hydrotreatment before desulfurization.Described " diesel fuel " means boiling range is the hydrocarbon mixture of 170 DEG C to 450 DEG C or the liquid of its any fractional composition.This type of hydrocarbon-containifluids fluids includes but not limited to light cycle oil, kerosene, straight-run diesel oil and hydroprocessed diesel etc. and combination thereof.
Term used herein " sulphur " represents any type of element sulphur if hydrocarbon-containifluids fluids is as the organosulfur compound existed normal in cracking gasoline or diesel fuel.The sulphur existed in hydrocarbon-containifluids fluids of the present invention includes but not limited to carbonyl sulfide (COS), carbon disulfide (CS2), mercaptan or other thiophenes etc. and combination thereof, especially thiophene, benzothiophene, alkylthrophene, alkyl benzothiophenes and methyldibenzothiophene is comprised, and the thiophenes that in diesel fuel, the normal molecular weight existed is larger.
Containing silicon nitride component in the composition of desulfurization of hydrocarbon oil catalyst provided by the invention, this component not easily reacts with zinc oxide component and acts in the repeatedly reaction and regenerative process of catalyst, can not produce zinc silicate material and make this desulfurization of hydrocarbon oil catalyst reduce because losing zinc oxide desulphurizing activated.Catalyst of the present invention has very high desulphurizing activated, also has the character significantly increasing catalyst abrasion strength resistance simultaneously, is applicable to the sweetening process repeatedly reacted and regenerate of catalytically cracked gasoline or diesel fuel.
Below will be described the present invention by embodiment.
The desulfurization of hydrocarbon oil catalyst that embodiment and comparative example obtain adopts X-ray diffractometer (Siemens company D5005 type) to obtain XRD spectra, carries out structure determination, Cu target, K α radiation, solid probe, tube voltage 40kV, tube current 40mA.
In the following Examples and Comparative Examples, the composition of desulfurization of hydrocarbon oil catalyst calculates according to feeding intake.
Embodiment 1
The present embodiment is for illustration of the method preparing desulfurization of hydrocarbon oil catalyst of the present invention.
(1) carrier is prepared.By Zinc oxide powder (the Headhorse company of 4.43kg, purity 99.7 % by weight), SAPO-11 molecular sieve (the catalyst asphalt in Shenli Refinery of 0.88kg, containing butt 0.70kg) and 6.57kg deionized water mixing, stir the mixed serum obtaining zinc oxide and rectorite after 30 minutes;
Get boehmite 1.33kg (catalyst Nanjing branch company, containing butt 1.00kg) and silicon nitride (the purity > 99.0 % by weight of 2.06kg, α phase, Qinhuangdao one promise new high-tech material development corporation, Ltd.) be uniformly mixed, then adding deionized water 4.6kg mixes as after slurries, add the hydrochloric acid (chemical pure of 30 % by weight of 360ml again, Beijing Chemical Plant produces) make the pH=2.1 of slurries, 80 DEG C of aging 2h are warming up to after stirring acidifying 1h, stir 1h after adding the mixed serum mixing of zinc oxide and rectorite again and obtain carrier pulp,
Described carrier pulp adopts NiroBowenNozzleTower
tMthe spray dryer of model carries out spraying dry, and spraying dry pressure is 8.5 to 9.5MPa, and inlet temperature less than 500 DEG C, outlet temperature is about 150 DEG C.The microballoon obtained by spraying dry is dry 1h at 180 DEG C first, and then at 635 DEG C, roasting 1h obtains carrier;
(2) controlling catalyst precursor.By Nickelous nitrate hexahydrate (Beijing chemical reagents corporation of the carrier 3.51kg of 3.2kg, purity > 98.5 % by weight) and 0.6kg deionized water solution dipping, the macerate obtained is after 180 DEG C of dry 4h, at air atmosphere 635 DEG C of roasting 1h, obtained catalyst precarsor;
(3) reduce.By catalyst precarsor reductase 12 h at 425 DEG C in hydrogen atmosphere, obtain desulfurization of hydrocarbon oil catalyst A 1.
The chemical composition of A1 is: zinc oxide content is 44.3 % by weight, and silicon nitride content is 20.6 % by weight, SAPO-11 molecular sieve content is 7.0 % by weight, and alumina content is 10.0 % by weight, and nickel content is 18.1 % by weight.
Embodiment 2
The present embodiment is for illustration of the method preparing desulfurization of hydrocarbon oil catalyst of the present invention.
By boehmite 1.56kg (catalyst Nanjing branch company, containing butt 1.17kg) and the silicon nitride of 1.50kg be uniformly mixed, then adding deionized water 8.2kg mixes as after slurries, the hydrochloric acid adding 30 % by weight of 260ml again makes the pH=1.9 of slurries, is warming up to 80 DEG C of aging 2h after stirring acidifying 1h.After temperature reduces, add the Zinc oxide powder of 5.52kg and the SAPO-31 molecular sieve (catalyst asphalt in Shenli Refinery, containing butt 0.3kg) of 0.31kg again, and stir 1h and obtain carrier pulp.
Method with reference to embodiment 1 is carried out the spray drying forming of carrier pulp and introduces active component nickel, obtains desulfurization of hydrocarbon oil catalyst A 2 after reduction.
The chemical composition of A2 is: zinc oxide content is 55.2 % by weight, and silicon nitride content is 15.0 % by weight, SAPO-31 molecular sieve content is 3.0 % by weight, and alumina content is 11.7 % by weight, and nickel content is 15.1 % by weight.
Embodiment 3
The present embodiment is for illustration of the method preparing desulfurization of hydrocarbon oil catalyst of the present invention.
By SAPO-34 molecular sieve (the catalyst asphalt in Shenli Refinery of the Zinc oxide powder of 4.93kg, 0.63kg, containing butt 0.50kg), the deionized water mixing of the silicon nitride of 2.1kg and 8.8kg, stir the mixed serum obtaining zinc oxide, rectorite and silicon nitride after 30 minutes.
(Shandong Aluminum Plant produces to get boehmite 1.80kg, containing butt 1.36kg) and deionized water 4.6kg mix as after slurries, add the hydrochloric acid (chemical pure of 30 % by weight of 300ml, Beijing Chemical Plant produces) make the pH=2.5 of slurries, be warming up to 80 DEG C of aging 2h after stirring acidifying 1h.Stir 1h after adding the mixed serum of zinc oxide, rectorite and silicon nitride slurries again and obtain carrier pulp.
Method with reference to embodiment 1 carries out the spray drying forming of carrier pulp.
With reference to method Kaolinite Preparation of Catalyst precursor and the catalyst of embodiment 1, unlike, substitute Nickelous nitrate hexahydrate impregnated carrier with the solution of nickel nitrate and cobalt nitrate, introduce active component nickel and cobalt, after reduction, obtain desulfurization of hydrocarbon oil catalyst A 3.
The chemical composition of A3 is: zinc oxide content is 49.3 % by weight, and silicon nitride content is 16.0 % by weight, SAPO-34 molecular sieve content is 5.0 % by weight, and alumina content is 13.5 % by weight, and nickel content is 8.1 % by weight, and cobalt content is 8.1 % by weight.
Embodiment 4
The present embodiment is for illustration of the method preparing desulfurization of hydrocarbon oil catalyst of the present invention.
By SAPO-34 molecular sieve (the catalyst asphalt in Shenli Refinery of the Zinc oxide powder of 4.93kg, 0.63kg, containing butt 0.50kg), the deionized water mixing of the silicon nitride of 2.1kg and 8.8kg, stir the mixed serum obtaining zinc oxide, rectorite and silicon nitride after 30 minutes;
Get boehmite 1.80kg (Shandong Aluminum Plant produces, containing butt 1.36kg) and deionized water 4.6kg to mix as after slurries, the hydrochloric acid adding 30 % by weight of 300ml makes the pH=2.5 of slurries, is warming up to 80 DEG C of aging 2h after stirring acidifying 1h.Stir 1h after adding the mixed serum of zinc oxide, rectorite and silicon nitride again and obtain carrier pulp;
Method with reference to embodiment 1 is carried out the spray drying forming of carrier pulp and introduces active component nickel, obtains desulfurization of hydrocarbon oil catalyst A 4 after reduction.
The chemical composition of A4 is: zinc oxide content is 49.3 % by weight, and silicon nitride content is 16.0 % by weight, SAPO-34 molecular sieve content is 5.0 % by weight, and alumina content is 13.5 % by weight, and nickel content is 16.2 % by weight.
Comparative example 1
The deionized water of the Zinc oxide powder of 4.43kg and 6.57kg is mixed, stirs and obtain zinc oxide slurries after 30 minutes;
Get boehmite 1.81kg (catalyst Nanjing branch company, containing butt 1.36kg) and expanded perlite (the catalyst Nanjing branch company of 2.46kg, containing butt 2.40kg) be uniformly mixed, then add deionized water 4.6kg to mix, the hydrochloric acid adding 30 % by weight of 360ml again makes slurries pH=2.1, be warming up to 80 DEG C of aging 2h after stirring acidifying 1h, then after adding the mixing of zinc oxide slurries, stirring 1h obtains carrier pulp.
Method with reference to embodiment 1 is carried out the spray drying forming of carrier pulp and introduces active component nickel, obtains desulfurization of hydrocarbon oil catalyst B 1 after reduction.
The chemical composition of B1 is: zinc oxide content is 44.3 % by weight, and expanded perlite content is 24.0 % by weight, and alumina content is 13.6 % by weight, and nickel content is 18.1 % by weight.
Comparative example 2
(Shandong Aluminum Plant produces to get boehmite 1.56kg, containing butt 1.17kg) and the diatomite (containing butt 1.80kg) of 1.85kg be uniformly mixed, then add deionized water 8.2kg to mix, the hydrochloric acid adding 30 % by weight of 260ml again makes slurries pH=1.9, is warming up to 80 DEG C of aging 2h after stirring acidifying 1h.After temperature reduces, add the Zinc oxide powder of 5.52kg again and stir 1h and obtain carrier pulp.
Method with reference to embodiment 1 is carried out the spray drying forming of carrier pulp and introduces active component nickel, obtains desulfurization of hydrocarbon oil catalyst B 2 after reduction.
The chemical composition of B2 is: zinc oxide content is 55.2 % by weight, and diatomite content is 18.0 % by weight, and alumina content is 11.7 % by weight, and nickel content is 15.1 % by weight.
Comparative example 3
The deionized water of the Zinc oxide powder of 4.93kg and 5.57kg is mixed, stirs and obtain zinc oxide slurries after 30 minutes;
(Shandong Aluminum Plant produces to get boehmite 1.80kg, containing butt 1.35kg) and 2.16kg go to diatomite (Global Mining Industry company, containing butt 2.10kg) be uniformly mixed, then add deionized water 4.6kg to mix, the hydrochloric acid adding 30 % by weight of 300ml again makes slurries pH=2.5, is warming up to 80 DEG C of aging 2h after stirring acidifying 1h.Stir 1h after adding the mixing of zinc oxide slurries again and obtain carrier pulp.
Method with reference to embodiment 3 is carried out the spray drying forming of carrier pulp and introduces active component nickel and cobalt, obtains desulfurization of hydrocarbon oil catalyst B 3 after reduction.
The chemical composition of B3 is: zinc oxide content is 49.3 % by weight, and diatomite content is 21.0 % by weight, and alumina content is 13.5 % by weight, and nickel content is 8.1 % by weight, and cobalt content is 8.1 % by weight.
Comparative example 4
The deionized water of the Zinc oxide powder of 4.93kg and 5.57kg is mixed, stirs and obtain zinc oxide slurries after 30 minutes;
(Shandong Aluminum Plant produces to get boehmite 1.80kg, containing butt 1.35kg) and kaolin (the Kaolin of Suzhou factory of 2.84kg, containing butt 2.10kg) be uniformly mixed, then add deionized water 3.6kg to mix, the hydrochloric acid adding 30 % by weight of 300ml again makes slurries pH=2.5, is warming up to 80 DEG C of aging 2h after stirring acidifying 1h.Stir 1h after adding the mixing of zinc oxide slurries again and obtain carrier pulp.
Method with reference to embodiment 1 is carried out the spray drying forming of mixing taste and is introduced active component nickel, obtains desulfurization of hydrocarbon oil catalyst B 4 after reduction.
The chemical composition of B4 is: zinc oxide content is 49.3 % by weight, and kaolin content is 21.0 % by weight, and alumina content is 13.5 % by weight, and nickel content is 16.2 % by weight.
Embodiment 5
(1) abrasion strength resistance evaluation.Abrasion strength resistance test is carried out to desulfurization of hydrocarbon oil catalyst A 1-A4 and B1-B4.Adopt straight tube wearing and tearing method, method, with reference to RIPP29-90 in " Petrochemical Engineering Analysis method (RIPP) experimental technique ", the results are shown in Table 1.Test the numerical value obtained less, show that abrasion strength resistance is higher.What in table 1, abrasion index was corresponding is fine powder generates when wearing and tearing under certain condition percentage.
(2) desulfurization performance evaluation.Adopting the micro-anti-experimental provision of fixed bed to carry out HDS evaluation experiment to desulfurization of hydrocarbon oil catalyst A 1-A4 and B1-B4, is 30mm, long in the fixed bed reactors of 1m by the desulfurization of hydrocarbon oil Catalyst packing of 16 grams at internal diameter.Raw material hydrocarbon ils is the catalytically cracked gasoline of sulphur concentration 780ppm, and reaction pressure is 1.38MPa, and hydrogen flowing quantity is 6.3L/h, and gasoline flow is 80mL/h, and reaction temperature is 410 DEG C, and the weight space velocity of raw material hydrocarbon ils is 4h
-1, carry out the desulphurization reaction of hydrocarbon oil containing surphur.Weigh desulphurizing activated with sulfur content in product gasoline.In product gasoline, sulfur content is by off-line chromatogram analysis method, adopts the GC6890-SCD instrument of An Jielun company to measure.In order to accurate characterization goes out the activity of desulfurization of hydrocarbon oil catalyst in industrial actual motion, HDS evaluation tested after catalyst carry out under the air atmosphere of 550 DEG C regeneration process.Desulfurization of hydrocarbon oil catalyst is carried out HDS evaluation experiment, and after regenerating 6 circulations, its activity settles out substantially, represents the activity of catalyst with the sulfur content in the product gasoline after catalyst the 6th stable circulation, and after stable, in product gasoline, sulfur content is as shown in table 1.
The motor octane number (MON) of gasoline and research octane number (RON) (RON) before adopting GB/T503-1995 and GB/T5487-1995 to measure reaction respectively and after the 6th stable circulation, the results are shown in Table 1.
Table 1
| Catalyst | A1 | A2 | A3 | A4 | B1 | B2 | B3 | B4 |
| Abrasion index | 2.7 | 3.3 | 2.9 | 3.0 | 7.0 | 7.8 | 7.4 | 7.4 |
| Product gasoline sulfur content/ppm | 8 | 4 | 6 | 6 | 10 | 5 | 8 | 7 |
| △MON | 0.50 | 0.15 | 0.35 | 0.30 | -0.50 | -0.45 | -0.50 | -0.45 |
| △RON | 0.45 | 0.05 | 0.30 | 0.30 | -0.45 | -0.35 | -0.40 | -0.45 |
| △(RON+MON)/2 | 0.48 | 0.10 | 0.33 | 0.30 | -0.48 | -0.40 | -0.45 | -0.45 |
Note:
1, the sulfur content of feed gasoline is 780ppm, RON be 93.0, MON is 82.7.
2, △ MON represents the value added of product MON;
3, △ RON represents the value added of product RON;
4, △ (RON+MON)/2 is the difference of product anti-knock index and raw material anti-knock index.
As can be seen from the result data of table 1, containing silicon nitride component in desulfurization of hydrocarbon oil catalyst provided by the invention, desulfurization of hydrocarbon oil catalyst has better desulphurizing activated and activity stability.Desulphurization catalyst has better abrasion strength resistance, thus makes desulphurization catalyst have longer service life.
Embodiment 6
Carry out aging to desulfurization of hydrocarbon oil catalyst A 1-A4 and B1-B4, condition is: catalyst is positioned over 600 DEG C, steam partial pressure is process 16h under the atmosphere of 20kPa.
Carry out XRD spectra analysis to A1-A4 and B1-B4 of aging front and back, Fig. 1 is the XRD spectra before and after A1 hydrothermal aging, and Fig. 2 is the XRD spectra before and after B1 hydrothermal aging.A2-A4 and A1 has similar XRD spectra, does not show; B2-B4 and B1 has similar XRD spectra, does not show.In FIG, do not occur in the XRD spectra after A1 hydrothermal aging 2 θ=22.0 of zinc silicate, 25.54, the characteristic peak of 48.9 and 59.4; In fig. 2, there is the above-mentioned characteristic peak of zinc silicate in the XRD spectra after B1 hydrothermal aging.Adopt the zinc silicate content in the XRD spectra of crystal content quantitative analysis B1-B4, the results are shown in Table 2.
With the evaluation method identical with embodiment 5 evaluate aging after the desulfurization performance of A1-A4 and B1-B4, the results are shown in Table 2.
Table 2
| Catalyst | A1 | A2 | A3 | A4 | B1 | B2 | B3 | B4 |
| Zinc silicate content/% by weight | 0 | 0 | 0 | 0 | 23.4 | 18.6 | 19.2 | 20.1 |
| Product gasoline sulfur content/ppm | 12 | 6 | 9 | 8 | 50 | 36 | 44 | 44 |
| △MON | 0.45 | 0.10 | 0.25 | 0.30 | -0.45 | -0.40 | -0.40 | -0.45 |
| △RON | 0.45 | 0.10 | 0.25 | 0.25 | -0.40 | -0.35 | -0.40 | -0.35 |
| △(RON+MON)/2 | 0.45 | 0.10 | 0.25 | 0.28 | -0.43 | -0.38 | -0.40 | -0.40 |
From the results shown in Table 2, after ageing process, in the desulfurization of hydrocarbon oil catalyst of embodiment, do not generate zinc silicate, and the catalyst in comparative example, zinc oxide can generate zinc silicate with the material of silicon oxide-containing, thus makes the desulphurizing activated reduction of catalyst.
Claims (18)
1. a desulfurization of hydrocarbon oil catalyst, with the gross weight of this desulfurization of hydrocarbon oil catalyst for benchmark, this desulfurization of hydrocarbon oil catalyst contains:
1) at least one of 10-80 % by weight is selected from the metal oxide of IIB, VB and group vib element;
2) aluminium oxide of 3-35 % by weight;
3) silicon nitride of 5-40 % by weight;
4) metallic promoter agent of 5-30 % by weight, described metallic promoter agent is selected from least one in cobalt, nickel, iron and manganese;
5) the SAPO molecular sieve of 1-20 % by weight.
2. desulfurization of hydrocarbon oil catalyst according to claim 1, wherein, the content of described metal oxide is 40-60 % by weight, the content of aluminium oxide is 8-15 % by weight, the content of silicon nitride is 12-25 % by weight, the content of described metallic promoter agent is 12-20 % by weight, and the content of described SAPO molecular sieve is 2-10 % by weight.
3. desulfurization of hydrocarbon oil catalyst according to claim 1 and 2, wherein, silicon nitride is α phase silicon nitride.
4. desulfurization of hydrocarbon oil catalyst according to claim 1 and 2, wherein, described metal oxide is at least one in zinc oxide, molybdenum oxide and vanadium oxide.
5. desulfurization of hydrocarbon oil catalyst according to claim 1 and 2, wherein, described SAPO molecular sieve is at least one in SAPO-5, SAPO-11, SAPO-31, SAPO-34 and SAPO-20.
6. the preparation method of the desulfurization of hydrocarbon oil catalyst in claim 1-5 described in any one, the method comprises:
(1) silicon nitride, alumina binder, at least one are selected from the metal oxide of IIB, VB and group vib element, SAPO molecular sieve, water and acidic liquid mixing, and the carrier pulp be mixed to get is carried out shaping, first dry, the first roasting, obtain carrier;
(2) in described carrier, introduce the precursor of metallic promoter agent, then carry out second dry and the second roasting, obtain catalyst precarsor;
(3) described catalyst precarsor is reduced in a hydrogen atmosphere, obtain desulfurization of hydrocarbon oil catalyst.
7. preparation method according to claim 6, wherein, the process of step (1) described mixing comprises:
I the contact of silicon nitride, alumina binder, water and acidic liquid is formed slurries by ():
(ii) described slurries and SAPO molecular sieve, described metal oxide are mixed to get carrier pulp.
8. preparation method according to claim 6, wherein, the process of step (1) described mixing comprises:
A alumina binder, water and acidic liquid contact and form slurries by ():
B described slurries and SAPO molecular sieve, described metal oxide, silicon nitride are mixed to get carrier pulp by ().
9. according to the preparation method in claim 6-8 described in any one, wherein, described alumina binder is selected from least one in SB powder, hydrated alumina, Alumina gel, boehmite, false boehmite, hibbsite and amorphous hydroted alumina.
10. preparation method according to claim 6, wherein, the precursor of described metallic promoter agent is selected from least one in the acetate of metallic promoter agent, carbonate, nitrate, sulfate, rhodanate and oxide.
11. preparation methods according to claim 6, wherein, carrier are introduced the method for the precursor of metallic promoter agent for dipping or precipitation.
12. preparation methods according to claim 6, wherein, described acidic liquid is acid or aqueous acid, and described acid is selected from water-soluble inorganic acid and/or organic acid.
13. preparation methods according to claim 7 or 8, wherein, the consumption of described acidic liquid makes the pH value of described slurries be 1-5.
14. preparation methods according to claim 6, wherein, the temperature of described first drying is room temperature-400 DEG C, and the time of described first drying is 0.5-8h; The temperature of described first roasting is 400-700 DEG C, and the time of described first roasting is more than 0.5h.
15. preparation methods according to claim 6, wherein, the temperature of described second drying is 50-300 DEG C, and the time of described second drying is 0.5-8h; The temperature of described second roasting is 300-800 DEG C, and the time of described second roasting is 0.5-4h.
16. preparation methods according to claim 6, wherein, the temperature of described reduction is 300-600 DEG C, and the time of described reduction is 0.5-6h, and in described hydrogen atmosphere, hydrogen content is 10-60 volume %.
The desulfurization of hydrocarbon oil catalyst that preparation method in 17. claim 6-16 described in any one obtains.
The method of 18. 1 kinds of desulfurization of hydrocarbon oil, the method comprises: in a hydrogen atmosphere, by the desulfurization of hydrocarbon oil catalyst exposure in hydrocarbon oil containing surphur and claim 1-5 and 17 described in any one, the temperature of described contact is 350-500 DEG C, and the pressure of described contact is 0.5-4MPa.
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| CN107970941A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | A kind of method of desulfurization of hydrocarbon oil catalyst and preparation method thereof and desulfurization of hydrocarbon oil |
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