CN105312084B - A kind of method of desulfurization of hydrocarbon oil catalyst and preparation method thereof and desulfurization of hydrocarbon oil - Google Patents
A kind of method of desulfurization of hydrocarbon oil catalyst and preparation method thereof and desulfurization of hydrocarbon oil Download PDFInfo
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Abstract
The invention discloses the method for a kind of desulfurization of hydrocarbon oil catalyst and preparation method thereof He desulfurization of hydrocarbon oil.On the basis of the gross weight of the desulfurization of hydrocarbon oil catalyst, the desulfurization of hydrocarbon oil catalyst contains：1) 10 80 weight % at least one metal oxide selected from IIB, VB and group vib element；2) 3 35 weight % titanium dioxide；3) 5 40 weight % silicon nitride；4) 5 30 weight % metallic promoter agent, the metallic promoter agent are selected from least one of cobalt, nickel, iron and manganese；5) 1 20 weight % SAPO molecular sieve.The desulfurization of hydrocarbon oil catalyst has more preferable stability and Geng Gao desulphurizing activated, more preferable abrasion resistance properties, and service life is longer.
Description
Technical field
The present invention relates to the method for a kind of desulfurization of hydrocarbon oil catalyst and preparation method thereof He desulfurization of hydrocarbon oil, in particular it relates to
A kind of desulfurization of hydrocarbon oil catalyst, the desulfurization of hydrocarbon oil catalyst for preparing the method for desulfurization of hydrocarbon oil catalyst and being obtained by this method, with
And the method that desulfurization of hydrocarbon oil is carried out using the desulfurization of hydrocarbon oil catalyst.
Background technology
As people are to the pay attention to day by day of environmental protection, environmental regulation is also increasingly strict, and reduces the sulphur of gasoline and diesel oil
Content is considered as one of most important measure for improving air quality.Most of sulphur in China's gasoline products come from hot-working
Gasoline blending component, such as catalytically cracked gasoline.Therefore the reduction of sulfur content helps to reduce the production of China's gasoline in hot-working petroleum
The sulfur content of product.The existing gasoline products standard GB 17930-2011 in China《Motor petrol》It is required that on December 31st, 2013,
Sulfur content must drop to 50 μ g/g in gasoline products.And following gasoline product quality standard will be stricter.At this
In the case of kind, catalytically cracked gasoline has to pass through the requirement that deep desulfuration can just make gasoline products meet environmental protection.
At present, the process for deep desulphurization of oil product mainly selective two kinds of desulfurization of catalytic desulfurhydrogenation and catalytic hydrogenation absorption
Method.Catalytic hydrogenation absorption desulfurization is to realize under conditions of hydrogen to inhale in the sulfide in hydrocarbon ils in certain temperature, pressure and facing
Attached removing, the technology have the characteristics of low and to hydrogen the purity requirement of hydrogen consumption is not high so that the technology is in terms of fuel desulfuration
Have broad application prospects.
CN1355727A discloses a kind of combination of adsorbents suitable for removing sulphur from cracking gasoline and diesel fuel
Thing, be made up of zinc oxide, silica, titanium dioxide and nickel, wherein nickel with substantially reduce valence state presence, its amount can from
Sulphur is removed in the cracking gasoline or diesel fuel stream that are contacted under desulfurization condition with the nickeliferous adsorbent composition.Said composition
It is granulated to form particle by the compound particles for forming zinc oxide, silica and titanium dioxide, dries, uses nickel or nickeliferous after roasting
Compound impregnates, and re-dry, roasting, reduction obtain.
CN1382071A discloses a kind of combination of adsorbents suitable for removing sulphur from cracking gasoline and diesel fuel
Thing, be made up of zinc oxide, silica, titanium dioxide and cobalt, wherein cobalt with substantially reduce valence state presence, its amount can from
Sulphur is removed in the cracking gasoline or diesel fuel stream that are contacted under desulfurization condition with the adsorbent composition containing cobalt.
US6150300 disclose it is a kind of prepare the method for adsorbent, including prepare spheric granules：(a) silica will be contained
Composition, the composition containing scattered metal oxide in an aqueous medium and the composition containing zinc oxide mix shape
First mixture is not extruded into the first mixture and；(b) forming the first mixture globulate has diameter 10-
1000mm particle.Wherein step (a) also includes mixing with metallic promoter agent.
CN1422177A discloses a kind of combination of adsorbents suitable for removing sulphur from cracking gasoline and diesel fuel
Thing, it is made up of zinc oxide, expanded perlite, titanium dioxide and promoter metals, wherein the promoter metals are with substantially also
Former valence state and the amount presence that sulphur can be removed when contacting under desulfurization conditions from cracking gasoline or diesel fuel stream.
CN1627988A discloses one kind and is suitable for removing elementary sulfur and vulcanization conjunction from cracking gasoline and diesel fuel
The adsorbent composition of thing, the adsorbent composition include：Zinc oxide, expanded perlite, aluminate and promoter metals, its
Described in promoter metals will cause from cracking when making cracking gasoline or diesel fuel stream contacts under desulfurization conditions with it
The amount of desulfurization in the stream of gasoline or diesel fuel is present, and at least partly described promoter metals exist with 0 valence state.
CN1856359A discloses a kind of method for producing composition, including：A) mixing liquid, zinc compound, containing two
Silica material, titanium dioxide and co-catalyst, to form its mixture；B) mixture is dried, is mixed with being formed through dry
Compound；C) this is calcined through dry mixture, to form the mixture through calcining；D) with appropriate reducing agent in appropriate condition
The lower mixture reduction by this through calcining, to produce the composition of the co-catalyst content in it with reduction valence state, and
E) recovery reorganization compound.Co-catalyst contains selected from various metals such as nickel.
CN1871063A discloses a kind of method for producing composition, and this method includes：A) by liquid, zinc compound,
Mixed containing earth silicon material, titanium dioxide to form its mixture；B) mixture is dried into the mixing to form
Once drying composite；C) described first is calcined to form first through calcining mixt through drying composite；D) by accelerator
Be attached to described first through within calcining mixt or on to form promoted mixture；E) make the promoted mixture with
Acid selected from citric acid, tartaric acid and combinations thereof is contacted to be formed through contact mixture；F) dried described through contact mixture
To form second through drying composite；G) described second is calcined to form second through calcining mixt through drying composite；h)
Suitable reducing agent reduction described second is used under suitable condition through calcining mixt to produce wherein containing reduction valence state
The composition of accelerator content, and i) reclaim the composition.
Although published adsorbent has certain desulfurization performance, with the raising of gasoline quality standard, to product
Content of sulfur in gasoline requirement is also constantly strict.And abrasion easily occurs in use for such catalyst, it is necessary to be continuously replenished
Catalyst, improve operating cost.As can be seen here, it is desirable to provide a kind of that there is more high desulfurization activity and the new of abrasion resistance properties to urge
Agent.
The content of the invention
The invention aims to overcome the desulphurizing activated low, structural instability of the adsorbent of prior art and wear resistance
Can be poor the defects of, there is provided the method for a kind of desulfurization of hydrocarbon oil catalyst and preparation method thereof and desulfurization of hydrocarbon oil.
To achieve these goals, the present invention provides a kind of desulfurization of hydrocarbon oil catalyst, with the total of the desulfurization of hydrocarbon oil catalyst
On the basis of weight, the desulfurization of hydrocarbon oil catalyst contains：1) 10-80 weight % at least one is selected from IIB, VB and group vib element
Metal oxide；2) 3-35 weight % titanium dioxide；3) 5-40 weight % silicon nitride；4) 5-30 weight % metal promotees
Enter agent, the metallic promoter agent is selected from least one of cobalt, nickel, iron and manganese；5) 1-20 weight % SAPO molecular sieve.
Present invention also offers the preparation method of the desulfurization of hydrocarbon oil catalyst of the present invention, this method includes：(1) by titanium dioxide
Titanium binding agent, water and acidic liquid mixing, obtain titanium colloidal sol；(2) by the titanium colloidal sol, silicon nitride, it is at least one selected from IIB,
The metal oxide of VB and group vib element, SAPO molecular sieve and water mixing, and by the carrier pulp being mixed to get carry out into
Type, the first drying, the first roasting, obtain carrier；(3) precursor of metallic promoter agent is introduced in the carrier, then carries out the
Two dryings and the second roasting, obtain catalyst precarsor；(4) catalyst precarsor is reduced in a hydrogen atmosphere, obtains hydrocarbon ils
Desulphurization catalyst.
Present invention also offers desulfurization of hydrocarbon oil catalyst made from preparation method provided by the present invention.
The invention provides a kind of method of desulfurization of hydrocarbon oil, this method includes：In a hydrogen atmosphere, by hydrocarbon oil containing surphur and this
The desulfurization of hydrocarbon oil catalyst contact that invention provides, the temperature of the contact is 350-500 DEG C, and the pressure of the contact is 0.5-
4MPa。
Containing stable silicon nitride in the composition of desulfurization of hydrocarbon oil catalyst provided by the invention, reduce and the gold such as zinc oxide
Belong to the dependent interaction of oxide, avoid the formation of silicic acid zinc material, such as the desulfurization of hydrocarbon oil of the acquisition of embodiment 1 that Fig. 1 show
The characteristic peak of zinc silicate is not present in XRD spectra after catalyst A1 hydrothermal aging.Desulfurization of hydrocarbon oil catalysis provided by the invention
Agent has that more preferable stability and Geng Gao's is desulphurizing activated, more effectively can inhale the sulphur in hydrocarbon ils during desulfurization of hydrocarbon oil
It is attached on desulfurization of hydrocarbon oil catalyst, obtains the lower hydrocarbon ils of sulfur content.And desulfurization of hydrocarbon oil catalyst provided by the invention has
More preferable abrasion resistance properties, catalyst attrition is lower in sweetening process, and service life is longer.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is XRD spectrums of the obtained desulfurization of hydrocarbon oil catalyst A1 of embodiment 1 before and after hydrothermal aging；
Fig. 2 is XRD spectrums of the obtained desulfurization of hydrocarbon oil catalyst B1 of comparative example 1 before and after hydrothermal aging.
Embodiment
The embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The present invention provides a kind of desulfurization of hydrocarbon oil catalyst, on the basis of the gross weight of the desulfurization of hydrocarbon oil catalyst, the hydrocarbon ils
Desulphurization catalyst contains：1) 10-80 weight % at least one metal oxide selected from IIB, VB and group vib element；2)3-
35 weight % titanium dioxide；3) 5-40 weight % silicon nitride；4) 5-30 weight % metallic promoter agent, the metal promoted
Agent is selected from least one of cobalt, nickel, iron and manganese；5) 1-20 weight % SAPO molecular sieve.
Preferably, on the basis of the gross weight of the desulfurization of hydrocarbon oil catalyst, the content of the metal oxide is 25-70 weights
% is measured, the content of titanium dioxide is 6-25 weight %, and the content of silicon nitride is 10-30 weight %, and the metallic promoter agent contains
Measure as 8-25 weight %, the content of the SAPO molecular sieve is 1-10 weight %.
It is highly preferred that on the basis of the gross weight of the desulfurization of hydrocarbon oil catalyst, the content of the metal oxide is 40-60
Weight %, the content of titanium dioxide is 8-15 weight %, and the content of silicon nitride is 12-25 weight %, the metallic promoter agent
Content is 12-20 weight %, and the content of the SAPO molecular sieve is 2-10 weight %.
According to the present invention, silicon nitride is white powder, and silicon nitride can be α phase silicon nitrides and/or beta phase silicon nitride, preferably
In the case of, silicon nitride is α phase silicon nitrides.The particle diameter of alpha-silicon nitride powders can be preferably (i.e. 6.5-25 μ between 2000-500 mesh
m)。
Desulfurization of hydrocarbon oil catalyst provided by the invention contains silicon nitride, can be effectively prevented from carrying out desulfurization of hydrocarbon oil process
In the catalyst composition in form zinc silicate, ensure the catalyst have preferably it is desulphurizing activated.Preferably, the desulfurization of hydrocarbon oil
There is no the characteristic peak of zinc silicate at 2 θ is 22.0,25.54,48.9 and 59.4 in XRD spectra of the catalyst after hydrothermal aging.
The hydrothermal aging is 500-700 DEG C of temperature, steam partial pressure 10-30kPa, processing time 10-24h.
According to the present invention, the SAPO molecular sieve is nearly body silicoaluminophosphate, is that silicon is introduced into aluminum phosphate skeleton to obtain
, its skeleton is by PO4 +、AlO4 -And SiO2Tetrahedron forms.This molecular sieve analog includes 13 kinds of three-dimensional microporous framework structures, and its hole is big
It is small to bePore volume is 0.18-0.48cm3/g.Under preferable case, the SAPO molecular sieve be SAPO-5, SAPO-11,
At least one of SAPO-31, SAPO-34 and SAPO-20.SAPO-5, SAPO-11, SAPO-31, SAPO-34 and SAPO-20
The hole size of molecular sieve is respectively(12 yuan of rings),(10 yuan of rings),(10 yuan of rings), (8 yuan of rings) and
(6 yuan of rings)；Pore volume is respectively 0.31,0.18,0.42,0.42 and 0.40cm3/g.Preferably, the SAPO molecular sieve is
SAPO-11, SAPO-31 and SAPO-34.
According to the present invention, at least one metal oxide selected from IIB, VB and group vib element can be zinc oxide,
At least one of cadmium oxide, vanadium oxide, niobium oxide tantalum oxide, chromium oxide, molybdenum oxide and tungsten oxide, it is described under preferable case
Metal oxide is at least one of zinc oxide, molybdenum oxide and vanadium oxide；Preferably, the metal oxide is zinc oxide.
In accordance with the present invention it is preferred that the metallic promoter agent is nickel and/or cobalt, the desulfurization of hydrocarbon oil catalyst can have
There is higher desulphurizing activated and regenerability；It is highly preferred that the metallic promoter agent is nickel.
In the present invention, titanium dioxide can be to provide cementation between each component in the desulfurization of hydrocarbon oil catalyst.And
Avoiding the desulfurization of hydrocarbon oil catalyst, al binder forms sharp crystalline substance with metal oxide when undergoing desulphurization reaction and regenerative process
Stone structure and make the desulfurization of hydrocarbon oil catalyst performance reduce the defects of.
Present invention also offers the preparation method of the desulfurization of hydrocarbon oil catalyst of the present invention, this method includes：(1) by titanium dioxide
Titanium binding agent, water and acidic liquid mixing, obtain titanium colloidal sol；(2) by the titanium colloidal sol, silicon nitride, it is at least one selected from IIB,
The metal oxide of VB and group vib element, SPAO molecular sieves and water mixing, and by the carrier pulp being mixed to get carry out into
Type, the first drying, the first roasting, obtain carrier；(3) precursor of metallic promoter agent is introduced in the carrier, then carries out the
Two dryings and the second roasting, obtain catalyst precarsor；(4) catalyst precarsor is reduced in a hydrogen atmosphere, obtains hydrocarbon ils
Desulphurization catalyst.
In the preparation method step (2) of desulfurization of hydrocarbon oil catalyst provided by the invention, the addition of the metal oxide can
Think with the addition of the powder type of the metal oxide, the metal oxide can also be added water be mixed into after slurries again with
The form of slurries adds.
In the case of, according to the invention it is preferred to, the titanium dioxide binding agent can be to be hydrolyzed in the acidic liquid, and
It is changed into the material of anatase titanium dioxide under conditions of the described first roasting.Preferably, the titanium dioxide binding agent
For in titanium tetrachloride, tetraethyl titanate, isopropyl titanate, acetic acid titanium, hydrous titanium oxide and anatase titanium dioxide extremely
Few one kind.Titanium dioxide binding agent contacts with excessive acid solution, can hydrolyze generation caking property colloidal solution.
In the present invention, at least one metal oxide, the SAPO molecules selected from IIB, VB and group vib element
Sieve, silicon nitride and metallic promoter agent are as described above, this is no longer going to repeat them.
According to the present invention, the acidic liquid can be the aqueous solution of acid or acid, and the acid can be selected from water-soluble
Inorganic acid and/or organic acid, preferably described acid can be at least one of hydrochloric acid, nitric acid, phosphoric acid and acetic acid.
According to the present invention, during step (1) described mixing, under preferable case, the dosage of the acidic liquid makes
The pH value of the slurries is 1-5, preferable ph 1.5-4.
In the present invention, the amount that step (1) adds water can be not specially limited, as long as the titanium colloidal sol can be obtained i.e.
Can.Such as it is 5-10 to add the amount of water with the weight ratio of titanium dioxide binding agent:1.
In the present invention, the carrier pulp that step (2) obtains can be the forms such as pastel or slurries.The carrier can be starched
Reshaping is dried after liquid thickening.More preferably the carrier pulp is slurry form, and it is 20- that can form granularity by spray drying
200 microns of microballoon, reach the purpose of shaping.For the ease of spray drying, the solid content of the carrier pulp is 10- before drying
50 weight %, preferably 20-50 weight %.There is no particular limitation for the amount of the water added in step (2), as long as obtained carrier
Slurries meet above-mentioned solid content.
In the present invention, the first drying means of carrier pulp and condition are known to those skilled in the art in step (2),
Such as dry method can be dry, dry, forced air drying.Under preferable case, the described first temperature dried can be room
Temperature is to 400 DEG C, preferably 100-350 DEG C；The time of first roasting is more than 0.5h, preferably 0.5-100h, more preferably
2-20h。
In the present invention, the first roasting condition of carrier pulp is also known to those skilled in the art in step (2), preferably
In the case of, the temperature of first roasting is 400-700 DEG C, preferably 450-650 DEG C；The time of first roasting is at least
0.5h, preferably 0.5-100h, more preferably 0.5-10h.
According to the present invention, step (3) is used to add metallic promoter agent.The precursor of the metallic promoter agent is can be second
It is changed into the material of the oxide of metallic promoter agent under roasting condition；Under preferable case, the precursor of the metallic promoter agent can be with
At least one of acetate, carbonate, nitrate, sulfate, rhodanate and oxide selected from metallic promoter agent.
In the case of, according to the invention it is preferred to, the method that the precursor of metallic promoter agent is introduced on carrier is dipping or precipitation.
The dipping can be the solution or suspension impregnation carrier with the precursor of metallic promoter agent；The precipitation can be to promote metal
The solution or suspension for entering the precursor of agent mix with carrier, then add ammoniacal liquor by the precursor precipitation of metallic promoter agent in carrier
On.
In the case of, according to the invention it is preferred to, the described second temperature dried is 50-300 DEG C, the described second time dried
For 0.5-8h；Preferably, the described second temperature dried is 100-250 DEG C, and the described second time dried was 1-5h；Described
The temperature of two roastings is 300-800 DEG C, and the time of second roasting is more than 0.5h；Preferably, the temperature of second roasting
Spend for 450-750 DEG C, the time of second roasting is 1-3h.Second roasting can be with the presence of oxygen or oxygen-containing gas
Lower progress, until volatile materials is removed and the precursor of metallic promoter agent is converted into the oxide shape of metallic promoter agent
Formula, obtain catalyst precarsor.
According to the present invention, in step (4), the oxide of the metallic promoter agent in the catalyst precarsor is changed into metal
Simple substance, the catalyst precarsor can be reduced under hydrogen atmosphere, metallic promoter agent is substantially deposited with reduction-state
Obtaining catalyst of the present invention.The condition of the reduction only turns the oxide of the metallic promoter agent in the catalyst precarsor
It is changed into metal simple-substance, and the metal oxide in the carrier will not change.Under preferable case, the temperature of the reduction is 300-
600 DEG C, time of the reduction is 0.5-6h, and the content of hydrogen is 10-60 volumes % in the hydrogen atmosphere；It is it is preferred that described
The temperature of reduction is 400 DEG C -500 DEG C, and the time of preferably described reduction is 1-3h.
In the present invention, step (4) can carry out catalyst precarsor reduction immediately after catalyst precarsor is made, can also
Carried out before use (before being adsorbed for desulfurization).Because metallic promoter agent easily aoxidizes, and the metal in catalyst precarsor promotees
Enter agent in the form of an oxide to exist, therefore catalyst precarsor is reduced and is carrying out desulfurization absorption for ease of transport, preferred steps (4)
Preceding progress.It is described to be reduced to make the metal in the oxide of metallic promoter agent substantially to exist with reduction-state, obtain the present invention's
Desulphurization catalyst.
It is the titanium dioxide binding agent, silicon nitride, the metal oxide, described in the case of, according to the invention it is preferred to
The addition of SAPO molecular sieve and the precursor of the metallic promoter agent causes in obtained desulfurization of hydrocarbon oil catalyst, with the hydrocarbon ils
On the basis of the gross weight of desulphurization catalyst, the metal oxide containing 10-80 weight %, 3-35 weight % titanium dioxide
Titanium, 5-40 weight % silicon nitride, the 5-30 weight % metallic promoter agent and 1-20 weight the % SAPO molecular sieve；
Preferably, the nitridation of the titanium dioxide, 10-30 weight % of the metal oxide, 6-25 weight % containing 25-70 weight %
The SAPO molecular sieve of silicon, the 8-25 weight % metallic promoter agent and 1-10 weight %；It is highly preferred that contain 40-60
The weight % metal oxide, 8-15 weight % titanium dioxide, 12-25 weight % silicon nitride, 12-20 weight %
The SAPO molecular sieve of the metallic promoter agent and 2-10 weight %.
Present invention also offers desulfurization of hydrocarbon oil catalyst made from preparation method provided by the present invention.
The invention provides a kind of method of desulfurization of hydrocarbon oil, this method includes：In a hydrogen atmosphere, by hydrocarbon oil containing surphur and this
The desulfurization of hydrocarbon oil catalyst contact that invention provides, the temperature of the contact is 350-500 DEG C, and the pressure of the contact is 0.5-
4MPa；Preferably, the temperature of the contact is 400-450 DEG C, and the pressure of the contact is 1.0-2.0MPa.Hydrocarbon in the process
Sulphur in oil is adsorbed on catalyst, so as to obtain the hydrocarbon ils of low sulfur content.
In the present invention, reacted catalyst can be reused after regeneration.The regeneration is carried out under oxygen atmosphere,
The condition of regeneration includes：The pressure of regeneration is normal pressure, and the temperature of regeneration is 400-700 DEG C, preferably 500-600 DEG C.
In the present invention, the catalyst after regeneration is before desulfurization of hydrocarbon oil is re-started, it is also necessary to reduced under hydrogen atmosphere,
The reducing condition of catalyst after regeneration includes：Temperature is 350-500 DEG C, preferably 400-450 DEG C；Pressure is 0.2-2MPa,
Preferably 0.2-1.5MPa.
In the present invention, the hydrocarbon ils includes cracking gasoline and diesel fuel, wherein " cracking gasoline " means that boiling range is 40
It is from making larger hydrocarbon molecule be cracked into heat or catalytic process compared with small molecule DEG C to 210 DEG C of hydrocarbon or its any cut
Product.Applicable thermal cracking process includes but is not limited to coking, thermal cracking and visbreaking etc. and combinations thereof.Applicable catalysis
The example of cracking process includes but is not limited to fluid catalystic cracking and RFCC etc. and combinations thereof.Therefore, it is applicable
Catalytically cracked gasoline include but is not limited to coker gasoline, pressure gasoline, visbreaker gasoil, fluid catalystic cracking gasoline and
Heavy oil cracked gasoline and combinations thereof.In some cases, in the methods of the invention as hydrocarbon-containifluids fluids when can be incited somebody to action before desulfurization
The cracking gasoline fractionation and/or hydrotreating." diesel fuel " means that the hydrocarbon that boiling range is 170 DEG C to 450 DEG C mixes
The liquid of thing or its any fractional composition.Such hydrocarbon-containifluids fluids include but is not limited to light cycle oil, kerosene, straight-run diesel oil and hydrogenation
Handle diesel oil etc. and combinations thereof.
Term used herein " sulphur " represents any type of element sulphur such as hydrocarbon-containifluids fluids such as cracking gasoline or diesel engine combustion
The organosulfur compound being commonly present in material.Sulphur present in hydrocarbon-containifluids fluids of the present invention includes but is not limited to carbonyl sulfide (COS), two
Nitric sulfid (CS2), mercaptan or other thiophenes etc. and combinations thereof, especially including thiophene, benzothiophene, alkylthrophene,
The bigger thiophene-based chemical combination of the molecular weight that is commonly present in alkyl benzothiophenes and methyldibenzothiophene, and diesel fuel
Thing.
Containing nitridation silicon components in the composition of desulfurization of hydrocarbon oil catalyst provided by the invention, the component is in the multiple of catalyst
Reaction and regenerative process in be not easy with the zinc oxide component effect of reacting, will not produce silicic acid zinc material urges the desulfurization of hydrocarbon oil
Agent reduces desulphurizing activated because losing zinc oxide.Catalyst of the present invention has very high desulphurizing activated, while also has obvious
Increase catalyst abrasion strength resistance property, be applicable to the reaction repeatedly and regeneration of catalytically cracked gasoline or diesel fuel
Sweetening process.
The present invention will be described in detail by way of examples below.
The desulfurization of hydrocarbon oil catalyst that embodiment and comparative example obtain uses X-ray diffractometer (Siemens companies D5005 types)
XRD spectra is obtained, carries out structure determination, Cu targets, 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 is calculated according to feeding intake.
Embodiment 1
The present embodiment is used for the method for preparing desulfurization of hydrocarbon oil catalyst for illustrating the present invention.
(1) carrier is prepared.2.40kg titanium tetrachloride (Beijing Chemical Plant, analyzing pure, 99 weight %) is slowly added to 4.6
Kilogram 5% watery hydrochloric acid, and be slowly stirred and avoid crystalline titanium dioxide from separating out, obtain the titanium colloidal sol pH=2.0 of pale yellow transparent；
By 4.43kg Zinc oxide powder (Headhorse companies, the weight % of purity 99.7), 0.88kg SAPO-11 points
Son sieve (catalyst asphalt in Shenli Refinery, containing butt 0.70kg), 2.06kg silicon nitride (weight %, the α phases of purity ＞ 99.0, Qin emperor
The promise new high-tech material development corporation, Ltd. of island one) and 8.80kg deionized water mixing, stirring 30 minutes after obtain zinc oxide, nitridation
The mixed serum of silicon and SAPO-11 molecular sieves；Then above-mentioned titanium colloidal sol is added, 1h is stirred after mixing and obtains carrier pulp；
The carrier pulp is used into Niro Bowen Nozzle TowerTMIt is dry that the spray dryer of model carries out spraying
Dry, spray drying pressure is 8.5 to 9.5MPa, and below 500 DEG C of inlet temperature, outlet temperature is about 150 DEG C.By being spray-dried
The microballoon arrived first dries 1h at 180 DEG C, and 1h is then calcined at 635 DEG C obtains carrier；
(2) catalyst precarsor processed.By 3.2kg carrier with 3.51kg Nickelous nitrate hexahydrate (Beijing chemical reagents corporation,
The weight % of purity ＞ 98.5) and 0.6kg deionized water solution dipping, obtained dipping thing is after 180 DEG C of dry 4h, in sky
635 DEG C of roasting 1h of gas atmosphere, are made catalyst precarsor；
(3) reduce.By catalyst precarsor in hydrogen atmosphere reductase 12 h at 425 DEG C, obtain desulfurization of hydrocarbon oil catalyst A1.
A1 chemical composition is：Zinc oxide content is 44.3 weight %, and silicon nitride content is 20.6 weight %, SAPO-11
Molecular sieve content is 7.0 weight %, and content of titanium dioxide is 10.0 weight %, and nickel content is 18.1 weight %.
Embodiment 2
The present embodiment is used for the method for preparing desulfurization of hydrocarbon oil catalyst for illustrating the present invention.
Titanium dioxide 1.25kg (Detitanium-ore-type, containing butt 1.17kg) is taken to be added to 1.8kg deionized water and 3.0kg
In 30 weight % hydrochloric acid (chemistry is pure, and Beijing Chemical Plant produces), pH=1.9, stirring reaction 1h, the titanium of pale yellow transparent is obtained
Colloidal sol；
By SAPO-11 molecular sieves (the catalyst asphalt in Shenli Refinery, containing butt of 1.50kg silicon nitride, 0.31kg
0.30kg), 5.52kg Zinc oxide powder and 10.0kg deionized water mix under agitation, obtain zinc oxide, SAPO-11
The mixed serum of molecular sieve and silicon nitride, then adds above-mentioned titanium colloidal sol and stirs 1h and obtain carrier pulp；
Method with reference to embodiment 1 carries out the spray drying forming of carrier pulp and introduces active component nickel, after reduction
To desulfurization of hydrocarbon oil catalyst A2.
A2 chemical composition is：Zinc oxide content is 55.2 weight %, and silicon nitride content is 15.0 weight %, SAPO-11
Molecular sieve content is 3.0 weight %, and content of titanium dioxide is 11.7 weight %, and nickel content is 15.1 weight %.
Embodiment 3
The present embodiment is used for the method for preparing desulfurization of hydrocarbon oil catalyst for illustrating the present invention.
Tetraethyl titanate 3.90kg (Aldrich, analyzing pure, 99 weight %) and 1.6kg deionized water is taken to stir
In the case of be slowly added into 3.8kg 10 weight % nitric acid (analysis pure, Beijing Chemical Plant produce) solution in, pH=2.3,
And 1h is stirred, obtain the titanium colloidal sol of pale yellow transparent；
By SAPO-34 molecular sieves (the catalyst asphalt in Shenli Refinery, containing butt of 4.93kg Zinc oxide powder, 0.63kg
0.50kg), 1.6kg silicon nitride and 10.8kg deionized water mix, and stirring obtains zinc oxide, SAPO-34 point after 30 minutes
The mixed serum of son sieve and silicon nitride, then add titanium colloidal sol and stir 1h and obtain carrier pulp；
The spray drying forming of carrier pulp is carried out with reference to the method for embodiment 1.
Catalyst precarsor and catalyst are prepared with reference to the method for embodiment 1, unlike, it is molten with nickel nitrate and cobalt nitrate
Liquid substitutes Nickelous nitrate hexahydrate impregnated carrier, introduces active component nickel and cobalt, desulfurization of hydrocarbon oil catalyst A3 is obtained after reduction.
A3 chemical composition is：Zinc oxide content is 49.3 weight %, and silicon nitride content is 16.0 weight %, SAPO-34
Molecular sieve content is 5.0 weight %, and content of titanium dioxide is 13.5 weight %, and nickel content is 8.1 weight %, cobalt content 8.1
Weight %.
Embodiment 4
The present embodiment is used for the method for preparing desulfurization of hydrocarbon oil catalyst for illustrating the present invention.
Tetraethyl titanate 3.90kg (Aldrich, analyzing pure, 99 weight %) and 1.6kg deionized water is taken to stir
In the case of be slowly added into 3.8kg 10 weight % nitric acid (analysis pure, Beijing Chemical Plant produce) solution in, pH=2.3,
And 1h is stirred, obtain the titanium colloidal sol of pale yellow transparent；
By SAPO-34 molecular sieves (the catalyst asphalt in Shenli Refinery, containing butt of 4.93kg Zinc oxide powder, 0.63kg
0.50kg), 1.6kg silicon nitride and 10.8kg deionized water mix, and stirring obtains zinc oxide, SAPO-34 point after 30 minutes
The mixed serum of son sieve and silicon nitride；Add titanium colloidal sol and stir 1h and obtain carrier pulp；
Method with reference to embodiment 1 carries out the spray drying forming of carrier pulp and introduces active component nickel, after reduction
To desulfurization of hydrocarbon oil catalyst A4.
A4 chemical composition is：Zinc oxide content is 49.3 weight %, and silicon nitride content is 16.0 weight %, SAPO-34
Molecular sieve content is 5.0 weight %, and content of titanium dioxide is 13.5 weight %, and nickel content is 16.2 weight %.
Comparative example 1
4.43kg Zinc oxide powder and 6.57kg deionized water are mixed, stirring obtains zinc oxide paste after 30 minutes
Liquid；
Take boehmite 1.81kg (catalyst Nanjing branch company, containing butt 1.36kg) and 2.46kg expanded perlite
(catalyst Nanjing branch company, containing butt 2.40kg) is stirred, and then adds deionized water 4.6kg and is well mixed, adds
360ml 30 weight % hydrochloric acid makes slurries pH=2.1, is warming up to 80 DEG C of aging 2h after stirring acidifying 1h, adds zinc oxide
Stirring 1h obtains carrier pulp after slurries mixing.
Method with reference to embodiment 1 carries out the spray drying forming of carrier pulp and introduces active component nickel, after reduction
To desulfurization of hydrocarbon oil catalyst B1.
B1 chemical composition is：Zinc oxide content is 44.3 weight %, and expanded perlite content is 24.0 weight %, oxidation
Al binder content is 13.6 weight %, and nickel content is 18.1 weight %.
Comparative example 2
Boehmite 1.56kg (Shandong Aluminum Plant produces, containing butt 1.17kg) and 1.85kg diatomite is taken (to contain butt
1.80kg) it is stirred, then adds deionized water 8.2kg and be well mixed, adding 260ml 30 weight % hydrochloric acid makes slurry
80 DEG C of aging 2h are warming up to after liquid pH=1.9, stirring acidifying 1h.5.52kg Zinc oxide powder is added after temperature reduction simultaneously
Stirring 1h obtains carrier pulp.
Method with reference to embodiment 1 carries out the spray drying forming of carrier pulp and introduces active component nickel, after reduction
To desulfurization of hydrocarbon oil catalyst B2.
B2 chemical composition is：Zinc oxide content is 55.2 weight %, and diatomite content is 18.0 weight %, and aluminum oxide glues
Knot agent content is 11.7 weight %, and nickel content is 15.1 weight %.
Comparative example 3
4.93kg Zinc oxide powder and 5.57kg deionized water are mixed, stirring obtains zinc oxide paste after 30 minutes
Liquid；
Take boehmite 1.80kg's (Shandong Aluminum Plant produces, containing butt 1.35kg) and 2.16kg to go to the diatomite (world
Mining company, containing butt 2.10kg) it is stirred, then add deionized water 4.6kg and be well mixed, add the 30 of 300ml
Weight % hydrochloric acid makes slurries pH=2.5, and 80 DEG C of aging 2h are warming up to after stirring acidifying 1h.After adding the mixing of zinc oxide slurries
Stirring 1h obtains carrier pulp.
Method with reference to embodiment 3 carries out the spray drying forming of carrier pulp and introduces active component nickel and cobalt, reduces
After obtain desulfurization of hydrocarbon oil catalyst B3.
B3 chemical composition is：Zinc oxide content is 49.3 weight %, and diatomite content is 21.0 weight %, and aluminum oxide glues
Knot agent content is 13.5 weight %, and nickel content is 8.1 weight %, and cobalt content is 8.1 weight %.
Comparative example 4
4.93kg Zinc oxide powder and 5.57kg deionized water are mixed, stirring obtains zinc oxide paste after 30 minutes
Liquid；
Take boehmite 1.80kg (Shandong Aluminum Plant produces, containing butt 1.35kg) and 2.84kg kaolin (Suzhou height
Ling Tu factories, containing butt 2.10kg) it is stirred, then add deionized water 3.6kg and be well mixed, add 300ml 30 weights
Amount % hydrochloric acid makes slurries pH=2.5, and 80 DEG C of aging 2h are warming up to after stirring acidifying 1h.Stirred after adding the mixing of zinc oxide slurries
Mix 1h and obtain carrier pulp.
Method with reference to embodiment 1 carries out mixing the spray drying forming of taste and introduces active component nickel, is obtained after reduction
Desulfurization of hydrocarbon oil catalyst B4.
B4 chemical composition is：Zinc oxide content is 49.3 weight %, and kaolin content is 21.0 weight %, and aluminum oxide glues
Knot agent content is 13.5 weight %, and nickel content is 16.2 weight %.
Embodiment 5
(1) abrasion strength resistance is evaluated.Abrasion strength resistance test is carried out to desulfurization of hydrocarbon oil catalyst A1-A4 and B1-B4.Using
Straight tube wears method, method reference《Petrochemical Engineering Analysis method (RIPP) experimental method》Middle RIPP 29-90, the results are shown in Table 1.Survey
The numerical value for trying to obtain is smaller, shows that abrasion strength resistance is higher.It is thin when wearing under certain condition corresponding to abrasion index in table 1
The percentage of powder generation.
(2) desulfurization performance is evaluated.Desulfurization of hydrocarbon oil catalyst A1-A4 and B1-B4 are entered using the micro- anti-experimental provision of fixed bed
Row HDS evaluation is tested, by 16 grams of desulfurization of hydrocarbon oil Catalyst packing in the fixed bed reactors that internal diameter is 30mm, a length of 1m.
Raw material hydrocarbon ils be sulphur concentration 780ppm catalytically cracked gasoline, reaction pressure 1.38MPa, hydrogen flowing quantity 6.3L/h, 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, carries out the desulphurization reaction of hydrocarbon oil containing surphur.
Weighed with sulfur content in product gasoline desulphurizing activated.Sulfur content is prompt using peace by offline chromatogram analysis method in product gasoline
The GC6890-SCD instruments of logical sequence company are measured.In order to which accurate characterization goes out desulfurization of hydrocarbon oil catalyst in industrial actual motion
Activity, the catalyst after the completion of HDS evaluation experiment carry out regeneration treatment under 550 DEG C of air atmosphere.Desulfurization of hydrocarbon oil is catalyzed
Agent carries out HDS evaluation experiment, and its activity settles out substantially after regenerating 6 circulations, after the 6th stable circulation of catalyst
Sulfur content in product gasoline represents the activity of catalyst, and sulfur content is as shown in table 1 in product gasoline after stablizing.
GB/T 503-1995 and GB/T 5487-1995 is respectively adopted to measure before reaction and gasoline after the 6th stable circulation
Motor octane number (MON) and research octane number (RON) (RON), the results are shown in Table 1.
Table 1
| Catalyst | A1 | A2 | A3 | A4 | B1 | B2 | B3 | B4 |
| Abrasion index | 2.5 | 2.9 | 2.7 | 2.7 | 7.0 | 7.8 | 7.4 | 7.4 |
| Product gasoline sulfur content/ppm | 6 | 4 | 4 | 5 | 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：
1st, the sulfur content of feed gasoline is 780ppm, RON 93.0, MON 82.7.
2nd, △ MON represent product MON value added；
3rd, △ RON represent product RON value added；
4th, △ (RON+MON)/2 is the difference of product anti-knock index and raw material anti-knock index.
It is can be seen that from the result data of table 1 in desulfurization of hydrocarbon oil catalyst provided by the invention containing nitridation silicon components, hydrocarbon
Oily desulphurization catalyst has more preferable desulphurizing activated and activity stability.Desulphurization catalyst has more preferable abrasion strength resistance, from
And desulphurization catalyst is set to have longer service life.
Embodiment 6
Aging is carried out to desulfurization of hydrocarbon oil catalyst A1-A4 and B1-B4, condition is：Catalyst is positioned over 600 DEG C, water steaming
Qi leel pressure is to handle 16h under 20kPa atmosphere.
XRD spectra analysis is carried out to the A1-A4 before and after aging and B1-B4, Fig. 1 is the XRD spectra before and after A1 hydrothermal agings,
Fig. 2 is the XRD spectra before and after B1 hydrothermal agings.A2-A4 has similar XRD spectra to A1, does not show；B2-B4 has similar to B1
XRD spectra, do not show.In Fig. 1, do not occur in the XRD spectra after A1 hydrothermal agings zinc silicate 2 θ=22.0,
25.54th, 48.9 and 59.4 characteristic peak；In fig. 2, there is the above-mentioned spy of zinc silicate in the XRD spectra after B1 hydrothermal agings
Levy peak.Using the silicic acid Zn content in crystal content quantitative analysis B1-B4 XRD spectra, 2 are the results are shown in Table.
With the A1-A4 and B1-B4 desulfurization performance after evaluation method evaluation aging same as Example 5, the results are shown in Table
2。
Table 2
| Catalyst | A1 | A2 | A3 | A4 | B1 | B2 | B3 | B4 |
| Silicic acid Zn content/weight % | 0 | 0 | 0 | 0 | 23.4 | 18.6 | 19.2 | 20.1 |
| Product gasoline sulfur content/ppm | 11 | 6 | 8 | 9 | 50 | 36 | 44 | 44 |
| △MON | 0.50 | 0.10 | 0.30 | 0.35 | -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 | 0.48 | 0.10 | 0.28 | 0.30 | -0.43 | -0.38 | -0.40 | -0.40 |
From the results shown in Table 2, after ageing process, without generation silicic acid in the desulfurization of hydrocarbon oil catalyst of embodiment
Zinc, and the catalyst in comparative example, zinc oxide can generate zinc silicate with the material of silicon oxide-containing, so that the desulfurization of catalyst is lived
Property reduce.
Claims (15)
1. a kind of desulfurization of hydrocarbon oil catalyst, on the basis of the gross weight of the desulfurization of hydrocarbon oil catalyst, the desulfurization of hydrocarbon oil catalyst contains
Have：
1) 10-80 weight % zinc oxide；
2) 3-35 weight % titanium dioxide；
3) 5-40 weight % silicon nitride；
4) 5-30 weight % metallic promoter agent, the metallic promoter agent are selected from least one of cobalt, nickel, iron and manganese；
5) 1-20 weight % SAPO molecular sieve.
2. desulfurization of hydrocarbon oil catalyst according to claim 1, wherein, using the gross weight of the desulfurization of hydrocarbon oil catalyst as base
Standard, the content of zinc oxide is 40-60 weight %, and the content of titanium dioxide is 8-15 weight %, and the content of silicon nitride is 12-25 weights
% is measured, the content of the metallic promoter agent is 12-20 weight %, and the content of the SAPO molecular sieve is 2-10 weight %.
3. desulfurization of hydrocarbon oil catalyst according to claim 1 or 2, wherein, silicon nitride is α phase silicon nitrides.
4. desulfurization of hydrocarbon oil catalyst according to claim 1 or 2, wherein, the SAPO molecular sieve is SAPO-5, SAPO-
11st, at least one of SAPO-31, SAPO-34 and SAPO-20.
5. the preparation method of the desulfurization of hydrocarbon oil catalyst in claim 1-4 described in any one, this method include：
(1) titanium dioxide binding agent, water and acidic liquid are mixed, obtains titanium colloidal sol；
(2) the titanium colloidal sol, silicon nitride, zinc oxide, SAPO molecular sieve and water are mixed, and the carrier pulp that will be mixed to get
Be molded, first dry, first roasting, obtain carrier；
(3) precursor of metallic promoter agent is introduced in the carrier, the second drying and the second roasting is then carried out, obtains catalyst
Precursor；
(4) catalyst precarsor is reduced in a hydrogen atmosphere, obtains desulfurization of hydrocarbon oil catalyst.
6. preparation method according to claim 5, wherein, the titanium dioxide binding agent is in the acidic liquid reclaimed water
Solution, and it is changed into the material of anatase titanium dioxide under conditions of being calcined described first.
7. preparation method according to claim 6, wherein, the titanium dioxide binding agent is selected from titanium tetrachloride, metatitanic acid
At least one of ethyl ester, isopropyl titanate, acetic acid titanium, hydrous titanium oxide.
8. preparation method according to claim 5, wherein, the method that the precursor of the metallic promoter agent is introduced on carrier
To impregnate or precipitating.
9. preparation method according to claim 5, wherein, the precursor of the metallic promoter agent is selected from the vinegar of metallic promoter agent
At least one of hydrochlorate, carbonate, nitrate, sulfate, rhodanate and oxide.
10. according to the method described in any one in claim 5-9, wherein, the acidic liquid is sour or acid the aqueous solution,
The acid is selected from water-soluble inorganic acid and/or organic acid, and the dosage of the acidic liquid makes the pH value of the titanium colloidal sol be
1-5。
11. preparation method according to claim 5, wherein, the described first temperature dried is -400 DEG C of room temperature, described the
One time dried was 0.5-8h；It is described first roasting temperature be 400-700 DEG C, it is described first roasting time for 0.5h with
On.
12. preparation method according to claim 5, wherein, the described second temperature dried is 50-300 DEG C, described second
The dry time is 0.5-8h；The temperature of second roasting is 300-800 DEG C, and the time of second roasting is 0.5-4h.
13. preparation method according to claim 5, wherein, the temperature of the reduction is 300-600 DEG C, the reduction
Time is 0.5-6h, and hydrogen content is 10-60 volumes % in the hydrogen atmosphere.
14. desulfurization of hydrocarbon oil catalyst made from the preparation method in claim 5-13 described in any one.
15. a kind of method of desulfurization of hydrocarbon oil, this method include：In a hydrogen atmosphere, by hydrocarbon oil containing surphur and claim 1-4 and 14
Desulfurization of hydrocarbon oil catalyst contact described in middle any one, the temperature of the contact is 350-500 DEG C, and the pressure of the contact is
0.5-4MPa。
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| CN103118782A (en) * | 2010-09-08 | 2013-05-22 | 庄信万丰股份有限公司 | Catalyst manufacturing method |
| CN103572277A (en) * | 2012-07-26 | 2014-02-12 | 北京赛亿科技股份有限公司 | Nanometer ceramic-based high temperature-resistant wear and corrosion-resistant self-cleaning composite coating |
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| CN103118782A (en) * | 2010-09-08 | 2013-05-22 | 庄信万丰股份有限公司 | Catalyst manufacturing method |
| CN103572277A (en) * | 2012-07-26 | 2014-02-12 | 北京赛亿科技股份有限公司 | Nanometer ceramic-based high temperature-resistant wear and corrosion-resistant self-cleaning composite coating |
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