The preparation method of Hydrobon catalyst
Technical field
The present invention relates to a kind of preparation method of hydrogenation catalyst, especially a kind of preparation side of body phase Hydrobon catalyst
Method.
Background technique
Currently, crude oil heaviness and in poor quality increasingly, the sustainable development of world economy and environmental regulation is increasingly tight in addition
Lattice need to produce a large amount of light clean fuels.Exploitation and using super-low sulfur even without sulphur vapour, diesel oil be within the scope of the world today it is clear
The trend of clean fuel development.Reaction temperature, hydrogen are such as improved by increasing reaction severity using traditional Hydrobon catalyst
The deep desulfuration even ultra-deep desulfurization of diesel oil also may be implemented in partial pressure or reduction reaction velocity etc., but reaction temperature is upper
It rises the variation that will lead to product colour and catalyst life shortens, and reducing air speed then means the reduction for the treatment of capacity.For existing
For some hydrogenation plants, design pressure has been fixed, and the amplitude for improving hydrogen partial pressure is limited.Therefore, currently by using
The catalyst of more high desulfurization activity is one of the important means of deep desulfuration.
Sulfur-containing compound in petroleum distillate containing various structures and different molecular weight, but in the ultra-deep desulfurization stage
(sulfur content is lower than 50 μ g/g), the mainly sulfur-containing compound of the substituted base such as removing 4,6- dimethyl Dibenzothiophene class.By
Make to produce steric hindrance between sulphur atom and the activated centre of catalyst in the adjacent methyl of sulphur atom, sulphur atom is not easy to connect
The activated centre of proximal response, thus lead to reaction rate sharp fall.
Conventional load type hydrogenation catalyst is limited by carrier pore structure, and active metal load capacity is usually no more than
30wt%, the activated centre quantity that loaded catalyst can be provided is limited, although can to activated centre number amount and type distribution
Adjustment is optimized, but since the limit bottleneck of activated centre quantity can not be broken through, the space for increasing substantially hydrogenation activity has
Limit, is difficult meet the needs of refinery is to V diesel product of producing country.The hydrogenation catalyst of body phase method preparation is most of by active gold
Belong to component to constitute, the limitation of tenor can be got rid of, can in any regulating catalyst each active component ratio, improve catalysis
The Hydrogenation of agent can be in the item for not improving device reaction severity since bulk phase catalyst has excellent hydrogenation activity
Under part, directly production meet National V emission standard without sulfur diesel product, the processing of device can be improved without transformation in original device
Amount reduces the production cost of refinery, realizes energy efficiency.
Body phase hydrogenation catalyst is divided into sulphided state body phase hydrogenation catalyst and oxidation state body phase hydrogenation catalyst.Oxidation state body
Phase catalyst preparation process is relatively easy, at low cost, industrial application, it mainly uses coprecipitation to prepare, with active gold
Belong to based on component, it typically is group VIB metallic elements (Mo, W) and group VIII metal element (Ni), and active metal atom is mutual
Staggeredly, reaction compartment is provided for reactant molecule, active metal is exposed to catalyst surface, provides reaction for reactant molecule and lives
Property center.Loaded catalyst is formed by mixing compared with low activity one kind activated centre with higher active two class activated centre
, and it is two class activated centres that bulk phase catalyst activated centre is substantially all, bulk phase catalyst mainly passes through increase catalyst
On activated centre density to greatly improving its catalytic activity.Chianelli etc. proposes spoke edge-seamed edge model to explain
The generation in unsupported catalyst activated centre, model is by MoS2/WS2The seamed edge active sites of crystal grain layer side edge are known as spoke edge position, mention
For adding hydrogen center, by MoS2/WS2The seamed edge active sites of crystal grain internal layer are known as seamed edge position, provide hydrogenolysis center.Therefore, catalyst
Add the distribution of hydrogen and hydrogenolysis activity and active sites closely related.
During the reaction, reactant molecule only reacts in its close catalyst surface, using existing total
The catalyst surface active metal dispersion of precipitation method preparation is uneven, while different hydrogenation active metals disorder distributions cause activity
There is no good coordinative role between metal, the metal of high-content is easy to happen metallic particles excess accumulation in bulk phase catalyst,
Reduce active mutually generation in this way, so that active metal is can't be hydrogenation sites, influence the benefit of the active metal of catalyst
With rate, and improve the use cost of catalyst.
CN1951561A discloses the method for preparing hydrogenation catalyst using co-precipitation, and catalyst uses active metal Ni, W
Component and precipitating reagent co-precipitation generate NixWyOzIt is molten aluminium salt can be added in above process in composite oxides precursor
Liquid, can also to be directly added into aluminium hydroxide after plastic, then with MoO3Mashing mixing, filtering, molding, activation are final catalysis
Agent.During this method prepares bulk phase catalyst, molybdenum oxide and NixWyOzComposite oxides are directly beaten mixing, lead to active gold
Belong to excess accumulation, reduces the quantity of active phase, reduce the utilization rate of active metal.
CN201410062726.8 discloses a kind of preparation method of non-loading type high-activity hydrogenation catalyst.This method is
The acid solution A for containing at least one group VIII metallic compound and at least one vib metals compound is first prepared, and
Alkaline solution B containing at least one silicon source or silicon source, two kinds of solution is slowly mixed together into precipitation reactor, in temperature 20
Coprecipitation reaction is carried out between ~ 120 DEG C, pH value 7 ~ 12, obtains slurries, and slurries are subjected to aging, suction filtration, washing, drying, molding
And calcination process, obtain catalyst.This method does not use conventional alkaline precipitating agent, but uses and contain a kind of silicon source or silicon source
Alkaline solution B do precipitating reagent, although this method changes precipitating reagent, but the active metal without changing bulk phase catalyst disperses
Property, active phase amount do not obviously increase, and the utilization rate of metal does not improve.
Ammonium hydrogen carbonate is added in body phase hydrogenation catalyst disclosed in CN102049265A during coprecipitated,
Carbon dioxide is added in body phase hydrogenation catalyst disclosed in CN102451703A during coprecipitated, generates carbonate or bicarbonate
Salt, the above method is that a certain amount of gas is released in roasting process using it, under the percussion of gas, increases catalysis
The Kong Rong of agent, specific surface area.Although this method under the percussion of gas, makes part metals active sites sudden and violent while reaming
It is exposed at the surface of catalyst, but catalyst pores easily collapse under gas effect, therefore, the effect to active metal dispersibility is improved
It is limited.
CN201510212110.9 discloses a kind of body phase Hydrobon catalyst and preparation method thereof.This method is using just
Addition prepares nickel aluminium mixed sediment, prepares tungsten, molybdenum and aluminium mixed sediment using parallel flow precipitation, then after the two is mixed it is old
Change after filtering obtained metal mixture and steam treatment and urea is added under appropriate conditions, the material warp after hydro-thermal process
Dry, molding, roasting obtain catalyst.Table phase active metallic content is high in the resulting bulk phase catalyst of this method, is easy excessive
Accumulation, to influence the active pattern and dispersibility for mutually accumulating pile layer.
Existing coprecipitation method is prepared in bulk phase catalyst technology, and different coprecipitation modes, Gelation Conditions can be living to catalyst
Property metal fit system, interaction relationship has very big between the distributions of hydrogenation active metals and different hydrogenation active metals
Influence, also result in vulcanization after bulk phase catalyst in MoS2/WS2Pattern occur it is apparent different.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of preparation methods of Hydrobon catalyst.This method preparation
Catalyst is a kind of body phase Hydrobon catalyst, and effective active is mutually more, and mutual facilitation is stronger, is had higher
Hydrodesulfurization and hydrodenitrogeneration reactivity worth, it is particularly suitable to be applied in diesel oil distillate ultra-deep hydrodesulfuration, denitrification reaction.
Under distillate ultra-deep hydrodesulfuration reaction environment, nitrogen-containing organic compound present in distillate is de- to hydrogen is added
Reaction of Salmon-Saxl generates apparent inhibiting effect, and hydrodesulfurization activity is reduced as the nitrogen content in raw material increases, this is because evaporating
Competitive Adsorption, the adsorption energy of nitrogenous compound occur on catalyst activity position for the nitrogenous compound and sulfur-containing compound divided in oil
Power is stronger, occupies the active sites on catalyst, and sulfur-containing compound is made to be difficult to approach, it is suppressed that hydrodesulfurization reaction, so
When the high heavy diesel of processing nitrogen content produces super-low sulfur product, the hydrodenitrogenationactivity activity that catalyst needs to have excellent, catalysis
The hydrodenitrogenationactivity activity of agent improves, and after nitrogen content reduces, the nitrogenous compound that competitive Adsorption occurs with sulfur-containing compound is reduced, and contains
Sulphur compound is easier, is also more adsorbed on catalyst activity position, promotes hydrodesulfurization reaction.Therefore, catalysis is improved
The hydrodenitrogenationactivity activity of agent has extremely important effect to the ultra-deep hydrodesulfuration activity for improving bulk phase catalyst.
The preparation method of Hydrobon catalyst provided by the invention, comprising:
(1), the mixed solution A containing Ni, W is prepared, the mixed solution B containing W, Mo, Al is prepared;
(2), mixed solution A and sodium metaaluminate alkaline solution cocurrent are added in reactor tank and carry out plastic reaction, generate it is nickeliferous,
Resulting slurries I are carried out aging by aluminium, tungsten sediment slurries I;
(3), mixed solution B and ammonium hydroxide cocurrent are added in the slurries I after aging and carry out plastic reaction, generate nickeliferous, molybdenum, tungsten,
Aluminum precipitation object slurries II, then proceed by aging;
(4), step (3) resulting material obtains Hydrobon catalyst through drying, molding, washing, then through drying, roasting;
Surfactant P1 is wherein added in step (2), surfactant P2 is added in step (3).
In the preparation method of Hydrobon catalyst of the present invention, surfactant P1 is selected from the anion that carbon number is C9 ~ C26
Surfactant is preferably selected from sulfonate type, carboxylic acid type, sulfuric ester salt form, sulfuric acid ester type, phosphate salt form, phosphate type
One of anionic surfactant is a variety of, is further selected from lignosulfonates, alkyl glyceryl ether sulfonate, succinic acid
Di-isooctyl sodium sulfonate, sodium alkyl benzene sulfonate, the oleic acid diethylene glycol dilaurate sulfonate, dibutyl naphthalene that carbon atom number is C10 ~ C16
Sodium sulfonate, methoxyl group fatty acyl amido benzene sulfonic acid sodium salt, aliphatic alcohol polyoxyvinethene phosphate, Monododecylphosphate potassium, palm fibre
Palmitic acid acid potassium, dodecylglycerol ether carboxylic acid sodium, α-sodium olefin sulfonate, the laurel alcohol sulfuric ester ammonium, the moon that carbon atom number is C14 ~ C18
One of cinnamic alcohol polyethenoxy ether sodium sulfate, two sodium sulphate of glyceryl monoacetate, lauramide sodium ethylsulfate etc. are a variety of.Table
Face activating agent P2 be selected from carbon number be less than C9 cationic surfactant, be preferably selected from dimethy lammonium chloride, diethyl ammonium halide,
One or more of halogenated methyl puratized agricultural spray, halogenation dimethyl puratized agricultural spray, halogenation trimethyl puratized agricultural spray etc., are further selected from dimethyl halogen
Change one or more of ammonium, halogenated methyl puratized agricultural spray, halogenation dimethyl puratized agricultural spray, wherein halogen is preferably chlorine.
In the preparation method of Hydrobon catalyst of the present invention, surfactant P1 can be before reactions in step (2)
And/or be added in reactor tank in reaction process, wherein be added before reaction i.e. mixed solution A and sodium metaaluminate alkaline solution simultaneously
Stream is added reactor tank and is first added in reactor tank before, is added in reaction process, it can independent cocurrent is added and/or mixes preparing
It is added when closing solution A.Surfactant P2 is added in step (3) to be added during the reaction, it can independent cocurrent adds
Enter and/or the addition when preparing mixed solution B, when preferably preparation mixed solution B is added.
It is acid solution in the mixed solution A of step (1), wherein weight concentration of the Ni in terms of NiO is 5~100g/L, excellent
It is selected as 10~80g/L, W is with WO3The weight concentration of meter is 2~60g/L, preferably 10~50g/L.Mixed solution B is acid molten
Liquid, wherein W is with WO3The weight concentration of meter is 2~70g/L, and preferably 4~60g/L, Mo is with MoO3The weight concentration 5 of meter~
80g/L, preferably 10~60g/L, Al is with Al2O3The weight concentration of meter is 2~60g/L, preferably 5~40g/L.It is mixed preparing
When closing solution A, the nickel source generally used can be one or more of nickel sulfate, nickel nitrate, nickel chloride;The tungsten generally used
Source is ammonium metatungstate.When preparing mixed solution B, for ammonium metatungstate, molybdenum source is ammonium molybdate in the tungsten source generally used, and silicon source can be with
For one or more of aluminum nitrate, aluminum sulfate, aluminium chloride and aluminium acetate etc..
The surfactant P1 being added in step (2), on the basis of the volume of mixed solution A, surfactant P1's adds
Entering amount is 5 ~ 60g/L, preferably 15 ~ 45g/L;The surfactant P2 being wherein added in step (3), with the body of mixed solution B
On the basis of product, the additional amount of surfactant P2 is 3~40g/L, preferably 5~25g/L.
In step (2), 40%~80% of W weight in catalyst is accounted for by the weight that mixed solution A is introduced into W in catalyst,
Preferably 51%~75%.
The concentration of sodium metaaluminate alkaline solution described in step (2) is with Al2O3It is calculated as 5 ~ 80g/L, preferably 10 ~ 60g/L.
In step (2), the reaction temperature of plastic is 20~90 DEG C, and preferably 30~70 DEG C, pH value control is 6.0 ~ 10.0,
Preferably 7.0 ~ 9.0, gelation time is 0.2 ~ 2.0 hour, preferably 0.3 ~ 1.5 hour.
The weight concentration of ammonium hydroxide described in step (3) is 5%~15%.
In step (3), 20%~60% of W weight in catalyst is accounted for by the weight that mixed solution B is introduced into W in catalyst,
Preferably 25%~49%.In step (3), by the weight that mixed solution B is introduced into Al account for total Al weight in catalyst 15%~
60%, preferably 25%~49%.
The reaction condition for carrying out plastic reaction is added in the slurries I after aging in step (3) mixed solution B and ammonium hydroxide cocurrent
Are as follows: reaction temperature is 20~90 DEG C, and preferably 30~80 DEG C, pH value control is 6.0 ~ 11.0, preferably 6.5 ~ 9.0, when plastic
Between be 0.5 ~ 4.0 hour, preferably 1.0 ~ 3.0 hours.
Aging condition described in step (2) is as follows: aging temperature is 40~90 DEG C, preferably 50~80 DEG C, when aging
PH value control is 6.0 ~ 8.0, preferably 6.5 ~ 7.5, and ageing time is 0.1 ~ 1.0 hour, preferably 0.2 ~ 0.8 hour.Aging
Carry out under stiring, preferred stirring condition is as follows: speed of agitator is 100~300 revs/min, preferably 150~250 revs/min.
Aging condition described in step (3) is as follows: aging temperature is 40~90 DEG C, preferably 50~80 DEG C, when aging
PH value control is 7.5 ~ 11.0, preferably 7.5 ~ 9.5, and ageing time is 1.5 ~ 6.0 hours, preferably 2.0 ~ 5.0 hours.Aging
Carry out under stiring, preferred stirring condition is as follows: speed of agitator is 300~500 revs/min, preferably 300~450 revs/min.
The pH value of the pH value of step (3) the described aging aging more described than step (2) is at least high by 0.5, preferably at least high by 1.0.
Drying, molding and washing described in step (4) can be carried out using conventional method in that art.Dried strip before molding
Part is as follows: 1 ~ 48 hour dry at 40 ~ 120 DEG C, preferably drying condition is as follows: 4 ~ 36 hours dry at 60 ~ 110 DEG C;It formed
Cheng Zhong can according to need and one of conventional shaping assistant, such as peptizing agent, extrusion aid etc. or a variety of is added.Described
Peptizing agent is one or more in hydrochloric acid, nitric acid, sulfuric acid, acetic acid, oxalic acid etc., and the extrusion aid, which refers to, is conducive to extrusion forming
One or more of substance, such as sesbania powder, carbon black, graphite powder, citric acid, the total material butt of the dosage Zhan of extrusion aid
1wt%~10wt%.Washing is usually used deionized water or containing decomposable salt (such as ammonium acetate, ammonium chloride, ammonium nitrate)
Solution washing, is washed till neutrality.
After formation, used drying and roasting can use this field normal condition to step (4), and drying condition is such as
Under: 1 ~ 48 hour dry at 50 ~ 250 DEG C, roasting condition is as follows: roasting 1 ~ 24 hour at 350 ~ 650 DEG C, preferably drying condition is such as
Under: 4 ~ 36 hours dry at 80 ~ 180 DEG C, preferably roasting condition is as follows: roasting 2 ~ 12 hours at 400 ~ 600 DEG C.
In the preparation method of Hydrobon catalyst of the present invention, required conventional catalyst can be added according to a conventional method and help
Agent, conven-tional adjuvants component such as Ti and/or Zr.It is preferably molten in preparation mixing in Hydrobon catalyst preparation process of the present invention
The compound containing adjuvant component, i.e. titanium source and/or zirconium source are added during liquid A.Titanium Nitrate, titanium sulfate, chlorination can be used in titanium source
One of titanium etc. is a variety of, and one of zirconium nitrate, zirconium chloride, zirconium oxychloride etc. or a variety of can be used in zirconium source.Based on the element
Weight content of the conven-tional adjuvants component in Hydrobon catalyst is 20% hereinafter, preferably 15% or less.
In the preparation method of Hydrobon catalyst of the present invention, the shape of catalyst can according to need for sheet, it is spherical,
Cylindrical bars and irregular strip (clover, bunge bedstraw herb), preferably cylindrical bars and irregular strip (clover, bunge bedstraw herb).Catalyst it is straight
Diameter can be the slice of 0.8 ~ 2.0mm and the thick item of > 2.5mm.
The resulting Hydrobon catalyst of step (4) of the present invention is oxidation state body phase Hydrobon catalyst, before use
It need to be vulcanized.The vulcanization is to convert corresponding sulfide for active metal W, Ni and Mo.The vulcanization process can
To be vulcanized using wet process, can also use dry pre-sulfiding.For the vulcanization process used in the present invention for wet process vulcanization, vulcanizing agent is normal
Rule vulcanization sulphur-containing substance used, can be organic sulfur-containing species, or inorganic sulphur-containing substance, such as sulphur, curing
One of carbon, dimethyl disulfide etc. are a variety of, and sulfurized oil is hydro carbons and/or distillate, and wherein hydro carbons is hexamethylene, ring penta
One of alkane, cycloheptane etc. are a variety of, and distillate is one of kerosene, normal line diesel oil, normal two wires diesel oil etc. or a variety of.
The dosage of vulcanizing agent is to make the sulphidity of each active metal in Hydrobon catalyst not less than 80%, can be according to practical progress
Adjustment, the dosage of vulcanizing agent can be needed for the theory of each active metal complete cure in Hydrobon catalyst sulfur content 80% ~
200%, preferably 100% ~ 150%.Presulfurization condition are as follows: volume is empty when 230 ~ 370 DEG C of temperature, 2.0 ~ 10MPa of Hydrogen Vapor Pressure, liquid
0.3 ~ 6.0h of speed-1, vulcanization time 3 ~ for 24 hours, preferably are as follows: volume is empty when 250 ~ 350 DEG C of temperature, 3.0 ~ 8.0MPa of Hydrogen Vapor Pressure, liquid
1.0 ~ 3.0h of speed-1, 5 ~ 16h of vulcanization time.
Hydrobon catalyst provided by the invention is body phase Hydrobon catalyst, and composition includes hydrogenation active metals
Component and aluminium oxide, hydrogenation active metal component WO3, NiO and MoO3, after vulcanizing, MoS2/WS2The average tap number of plies be
6.0 ~ 9.0 layers, preferably 6.5 ~ 9.0 layers, MoS2/WS2Lamella average length is 4.0 ~ 6.5nm, preferably 4.5 ~ 6.0nm.
Hydrobon catalyst of the invention, on the basis of the weight of Hydrobon catalyst, hydrogenation active metal component
W, total content of the Ni and Mo in terms of oxide is 40% ~ 91%, preferably 50% ~ 81%, and the content of aluminium oxide is 9% ~ 60%, preferably
19%~50%。
In Hydrobon catalyst of the invention, the molar ratio of W/Mo is 1:10 ~ 8:1, preferably 1:8 ~ 5:1, Ni/(Mo+
W) molar ratio is 1:12 ~ 12:1, preferably 1:8 ~ 8:1.
Hydrobon catalyst of the invention, after vulcanizing, MoS2/WS2It is as follows to accumulate number of plies distribution: the number of plies is 7.0 ~ 9.0
The piece number of plies account for the total tablet number of plies 60% ~ 85%, preferably 70% ~ 85%.Lamella distribution of lengths is as follows: length is the piece of 4.0 ~ 6.0nm
The number of plies accounts for the total tablet number of plies 55% ~ 85%, preferably 64% ~ 80%.
Hydrobon catalyst of the invention, after vulcanizing, MoS2/WS2It is as follows to accumulate number of plies distribution: the number of plies is less than 4.0
The piece number of plies accounts for the total tablet number of plies 1% ~ 5%, and the piece number of plies that the number of plies is 4.0 to less than 7.0 accounts for the total tablet number of plies 2% ~ 12%, and the number of plies is 7.0 ~
The 9.0 piece number of plies accounts for the total tablet number of plies 60% ~ 85%, and the piece number of plies of the number of plies greater than 9.0 accounts for the total tablet number of plies 5% ~ 25%.
Hydrobon catalyst of the invention, after vulcanizing, MoS2/WS2Lamella distribution of lengths is as follows: length is less than 2.0nm
The piece number of plies account for the total tablet number of plies 3.0% ~ 15.0%, the piece number of plies that length is 2.0 to less than 4.0nm account for the total tablet number of plies 5.0% ~
20.0%, the piece number of plies that length is 4.0 ~ 6.0nm accounts for the total tablet number of plies 55.0% ~ 85.0%, and length is greater than 6.0 to the lamella of 8.0nm
Number accounts for the total tablet number of plies 2.0% ~ 10.0%, and the piece number of plies of the length greater than 8.0nm accounts for the total tablet number of plies 0.1% ~ 3.0%.
The property of the Hydrobon catalyst is as follows: specific surface area is 180 ~ 500m20.20 ~ 0.80mL/ of/g, Kong Rongwei
g。
Vulcanization of the present invention is to convert active metal component W, Ni and Mo in corresponding sulfide to get vulcanization
State Hydrobon catalyst, the sulphidity of each active metal is not less than 80% in the catalyst.
It being can according to need in Hydrobon catalyst of the present invention containing adjuvant component, adjuvant component is titanium and/or zirconium, with
Weight content of the element meter adjuvant component in Hydrobon catalyst is 20% hereinafter, preferably 15% or less.
Hydrobon catalyst of the present invention, after vulcanizing, MoS2/WS2The number of plies for accumulating pile is high, and length is small, is particularly concentrated on
The number of plies is 6.0 ~ 9.0 layers, and chip length is 4.0 ~ 6.5nm, and the effective active of generation is mutually more, and mutual facilitation is more
By force, activity is higher, while high mechanical strength, is lost small in preparation process, has higher hydrodesulfurization and hydrodenitrogeneration reactivity
Can, it is suitable for being applied in diesel oil distillate ultra-deep hydrodesulfuration, denitrification reaction, is particularly suitable for the poor quality of processing high nitrogen high sulfur content
Diesel oil.
The method that the present invention prepares Hydrobon catalyst, being first will be containing Ni, the mixed solution A of part W and sodium metaaluminate
Alkaline solution cocurrent carries out coprecipitation reaction, wherein surfactant P1 is added before the reaction and/or in reaction, W, Ni, Al are mixed
It closes object slurries and carries out preliminary aging for the first time, generate the predecessor of biggish W, Ni, Al oxide of particle, surfactant P1's
Being added keeps W in predecessor and Ni evenly dispersed, and the hydrogenation active metals previously deposited are to the hydrogenation activity in rear deposition
Metal has certain anchoring effect, then mixed solution B, surfactant P2 and the ammonium hydroxide addition of remaining W, Mo, Al is above-mentioned
It is reacted in the slurries of aging, then carries out second of depth aging and prepare tungsten, molybdenum, nickel and aluminum precipitation object, be finally made and urge
Agent, after the addition of surfactant P2 is conducive to plus the metal of deposition more effectively carries out anchoring effect.By to preparation step
With the comprehensively control of preparation condition, during tungsten, molybdenum, nickel and aluminium mixed sediment particle growth, by active metal it
Between effectively anchoring act on, deposit different hydrogenation active metals in an orderly manner in the catalyst, control metal oxide particle increase
The probability to contact with each other between long speed and active metal, the granular size of W and Mo deposit are suitable for and obtain its distribution
Good control not only increases MoS in bulk phase catalyst2/WS2The accumulation number of plies, reduce lamella length, optimize active phase
The effective active of pattern, generation is mutually more, and mutual facilitation is stronger, and activity is higher, and pore structure is more advised
It is whole and unimpeded, be conducive to contact of the reactant molecule with activated centre, further increase hydrodesulfurization and denitrification activity.
It is with higher in the particularly suitable ultra-deep hydrodesulfuration and denitrification reaction as light fraction oil of the catalyst
Hydrodesulfurization and hydrodenitrogenationactivity activity, the especially heavy diesel of working process high nitrogen high sulfur content.In the heavier diesel fraction
Sulfur content be 1000~20000 μ g/g, wherein in thiophene and derivatives the content of sulphur account for the 60wt% of raw material total sulfur content~
85wt%, nitrogen content are that the content of nitrogen in 200~2000 μ g/g, wherein carbazole and its derivative accounts for the 60wt% of raw material total nitrogen content
~80wt%.
Specific embodiment
In the present invention, specific surface area and Kong Rong use low temperature liquid nitrogen determination of adsorption method, and mechanical strength is measured using side pressure method.
MoS in the present invention, in bulk phase catalyst2/WS2The accumulation number of plies, lamella length be by transmissioning electric mirror determining, wherein right
In W-Ni-Mo catalyst after vulcanizing, that be capable of forming stack layer is active phase MoS2And WS2, the present invention in MoS2/WS2Shape
Formula indicates active phase.Hydrobon catalyst of the invention refers to after vulcanizing by unvulcanised state Hydrobon catalyst sulphur
Sulphided state Hydrobon catalyst is turned to, that is, refers to sulphided state Hydrobon catalyst.In the present invention, wt% is mass fraction, and v% is
Volume fraction.
In the present invention, sulphidity is measured using X X-ray photoelectron spectroscopy X instrument (XPS), sulphided state active metal
Content account for the active metal total content percentage be the active metal sulphidity.
Embodiment 1
Nickel chloride, ammonium metatungstate, sodium lignin sulfonate are added to the dissolving tank 1 that deionized water is housed respectively, are configured to mix molten
Liquid A, weight concentration of the Ni in terms of NiO is 28g/L in mixed solution A, and W is with WO3The weight concentration of meter is 27g/L, sulfomethylated lignin
The weight concentration of sour sodium is 38g/L.Deionized water, ammonium metatungstate, ammonium molybdate, aluminium chloride are added into dissolving tank 2 to be uniformly mixed
Afterwards, alkyl dimethyl ammonium chloride is added and is configured to mixed solution B, W is in solution B with WO3The weight concentration of meter is 30g/L, and Mo is with MoO3
Meter weight concentration is 36g/L, and Al is with Al2O3The weight concentration of meter is 26g/L, and alkyl dimethyl ammonium chloride weight concentration is 15g/L.It will
Deionized water is added in reactor tank, is with Al by weight concentration2O3It is calculated as the sodium aluminate solution and mixed solution A cocurrent of 30g/L
It is added in reactor tank, gelling temperature is maintained at 56 DEG C, and pH value control is 7.8 in cocurrent plastic reaction process, gelation time control
At 50 minutes, nickeliferous, tungsten, aluminum precipitation object slurries I are generated.Sediment slurries I aging under stiring will be obtained, mixing speed is
180 revs/min, 75 DEG C of aging temperature, aging pH value is controlled 7.0, aging 0.6 hour.After aging, by mixed solution B, again
Measuring concentration is that 10wt% ammonium hydroxide cocurrent is added in slurries I, and gelling temperature is maintained at 64 DEG C, pH value control in cocurrent plastic reaction process
7.8, gelation time control obtained nickel, tungsten, molybdenum, aluminum precipitation object slurries II, sediment slurries II is being stirred system at 2.0 hours
Aging under the conditions of mixing, mixing speed are 400 revs/min, and 75 DEG C of aging temperature, pH value control, will 8.3, ageing time 3.0 hours
Slurries filtering after aging, filter cake is 8 hours dry at 110 DEG C, rolls, extruded moulding.5 times are washed with deionized at room temperature extremely
It is neutral.Then wet bar is 10 hours dry at 80 DEG C, and 500 DEG C roast 4 hours, obtains catalyst A.Catalyst composition and main character
It is shown in Table 1.
Embodiment 2
According to the method for embodiment 1, by the catalyst B in table 1 constituent content match, into dissolving tank 1 be added deionized water,
Nickel chloride, ammonium metatungstate, zirconium oxychloride, cetyl benzenesulfonic acid sodium are uniformly mixed, and prepare mixed solution A (wherein cetyl
The weight concentration of benzene sulfonic acid sodium salt is 39g/L), deionized water, aluminum nitrate, ammonium metatungstate, ammonium molybdate are added into dissolving tank 2, mixes
Close uniformly, be added methyl chloride puratized agricultural spray, prepare mixed solution B(wherein methyl chloride aniline weight concentration be 20g/L).It will go
Ionized water is added in reactor tank, by weight concentration with Al2O3The sodium aluminate solution and mixed solution A cocurrent for being calculated as 38g/L are added
In reactor tank, gelling temperature is maintained at 55 DEG C, and pH value control is 7.4 in cocurrent plastic reaction process, and gelation time control is 55
Minute, generate nickeliferous, tungsten, aluminium, zirconium sediment slurries I.It will obtain sediment slurries I aging under stiring, mixing speed 190
Rev/min, 72 DEG C of aging temperature, aging pH value is controlled 7.0, aging 0.7 hour.It is 10wt% by weight concentration after aging
Ammonium hydroxide and mixed solution B cocurrent are added in slurries I, and gelling temperature is maintained at 45 DEG C, and pH value controls in cocurrent plastic reaction process
8.0, gelation time control obtained nickel, tungsten, molybdenum, aluminium, zirconium sediment slurries II, by sediment at 2.5 hours after reaction
The aging under agitation of slurries II, mixing speed be 420 revs/min, ageing time 4.5 hours, 72 DEG C of aging temperature, aging pH
Value control is 8.3.By the slurries filtering after aging, filter cake is 12 hours dry at 100 DEG C, rolls, extruded moulding.It spends at room temperature
Ion water washing 4 times extremely neutral.Then wet bar is 10 hours dry at 90 DEG C, and 530 DEG C roast 4 hours, obtains catalyst B.Catalysis
Agent composition and main character are shown in Table 1.
Embodiment 3
According to the method for embodiment 1, by the catalyst C in table 1 constituent content match, into dissolving tank 1 be added nickel nitrate, partially
Ammonium tungstate, deionized water, be uniformly mixed, prepare mixed solution A, into dissolving tank 2 be added ammonium metatungstate, ammonium molybdate, aluminium chloride,
Deionized water is uniformly mixed, and chlorodimethyl puratized agricultural spray is added, and the weight for preparing mixed solution B(wherein Dimethylanilinium chloride is dense
Degree is 23g/L).Deionized water and Aerosol OT are added in reactor tank, Aerosol OT
Additional amount counted on the basis of the volume of mixed solution A, the weight concentration of Aerosol OT is 35g/L.It will weigh
Amount concentration is Al2O3The sodium aluminate solution and mixed solution A cocurrent of 45g/L is added in reactor tank, and gelling temperature is maintained at 60
DEG C, 7.8, gelation time control generated nickeliferous, tungsten, aluminum precipitation object at 70 minutes for pH value control in cocurrent plastic reaction process
Slurries I.It will obtain sediment slurries I aging under stiring, mixing speed is 220 revs/min, 78 DEG C of aging temperature, aging pH value
Control is 6.8, aging 0.8 hour.It is that slurries I is added in 8wt% ammonium hydroxide and mixed solution B cocurrent by weight concentration after aging
In, gelling temperature is maintained at 50 DEG C, in cocurrent plastic reaction process pH value control 8.2, gelation time control at 2.0 hours,
Nickel, tungsten, molybdenum, aluminium, sediment slurries II are obtained after reaction, by the aging under agitation of sediment slurries II, stirring speed
Degree is 450 revs/min, and ageing time 4.8 hours, 76 DEG C of aging temperature, aging pH value was controlled 8.6.By the slurries mistake after aging
Filter, filter cake is 15 hours dry at 70 DEG C, rolls, extruded moulding.6 times are washed with deionized at room temperature to neutrality.Then wet bar
12 hours dry at 90 DEG C, 480 DEG C roast 6 hours, obtain catalyst C.Catalyst composition and main character are shown in Table 1.
Embodiment 4
According to the method for embodiment 1, by the catalyst D in table 1 constituent content match, into dissolving tank 1 be added deionized water,
Nickel chloride, ammonium metatungstate, α-sodium olefin sulfonate (C atomicity is 16), are uniformly mixed, prepare mixed solution A (wherein α-alkenyl sulphur
The weight concentration of sour sodium is 30 g/L), deionized water, aluminium chloride, ammonium metatungstate, ammonium molybdate are added into dissolving tank 2, mixing is equal
It is even, be added methyl chloride puratized agricultural spray, prepare mixed solution B(wherein methyl chloride puratized agricultural spray weight concentration be 18g/L).By deionization
Water is added in reactor tank, by weight concentration with Al2O3Reaction is added in the sodium aluminate solution and mixed solution A cocurrent for being calculated as 32g/L
In tank, gelling temperature is maintained at 50 DEG C, in cocurrent plastic reaction process pH value control 8.0, gelation time control at 70 minutes,
Generate nickeliferous, tungsten, aluminum precipitation object slurries I.The sediment slurries I aging that will be obtained, 74 DEG C of aging temperature, the control of aging pH value exists
7.3, aging 0.5 hour.It is that 8wt% ammonium hydroxide and mixed solution B cocurrent are added in slurries I by weight concentration after aging, at
Glue temperature is maintained at 55 DEG C, and pH value control is 8.0 in cocurrent plastic reaction process, and gelation time control was at 2.4 hours, reaction knot
Nickel, tungsten, molybdenum, aluminum precipitation object slurries II are obtained after beam, by the aging under agitation of sediment slurries II, mixing speed 400
Rev/min, ageing time 4.1 hours, 75 DEG C of aging temperature, aging pH value was controlled 8.5.By the slurries filtering after aging, filter cake
It is 9 hours dry at 110 DEG C, it rolls, extruded moulding.4 times are washed with deionized at room temperature to neutrality.Then wet bar is dry at 90 DEG C
Dry 12 hours, 560 DEG C roasted 4 hours, obtained catalyst D.Catalyst composition and main character are shown in Table 1.
Comparative example 1
By method disclosed in CN1951561A, preparation and the catalyst of embodiment 1 form identical reference agent E, and detailed process is such as
Under:
It is formed by the catalyst of embodiment 1, nickel chloride and ammonium metatungstate preparation is dissolved in deionized water, are configured to mixed solution,
Wherein weight concentration of the Ni in terms of NiO is 28g/L, and W is with WO3The weight concentration of meter is 46g/L, and Al is with Al2O3The weight of meter is dense
Degree is 38g/L.500mL deionized water is added in reactor tank, is that reaction is added in 10wt% ammonium hydroxide and mixed solution cocurrent by concentration
Plastic is carried out in tank, gelling temperature is maintained at 60 DEG C, at the end of pH value control 7.8, gelation time control is raw at 3.0 hours
At nickeliferous, tungsten sediment slurries.Then aging is carried out, ageing time 3.8 hours, 75 DEG C of aging temperature, pH value controlled when aging
After 7.8, filtering, deionized water, aluminium hydroxide and molybdenum trioxide are added in filter cake, is beaten, after mixing, filters, filter
Cake is 8 hours dry at 100 DEG C, rolls, extruded moulding.It is washed with deionized at room temperature 5 times.Then wet bar is at 80 DEG C dry 10
Hour, 500 DEG C roast 4 hours, obtain catalyst E.Catalyst composition and main character are shown in Table 1.
Comparative example 2
It is formed by the catalyst of embodiment 1, aluminium chloride, nickel chloride, ammonium molybdate and ammonium metatungstate is dissolved in deionized water, are configured to
Mixed solution, wherein weight concentration of the Ni in terms of NiO is 28g/L, and W is with WO3The weight concentration of meter is 46g/L, and Mo is with MoO3Meter
Weight concentration is 27g/L, and Al is with Al2O3The weight concentration of meter is 38g/L.It is 10wt% ammonium hydroxide and mixed solution cocurrent by concentration
Be added reactor tank in carry out plastic, gelling temperature is maintained at 60 DEG C, at the end of pH value control 7.8, gelation time control is 3.0
Hour, generate tungstenic, nickel, molybdenum, aluminum precipitation object slurries.Then aging is carried out, ageing time 3.8 hours, 75 DEG C of aging temperature, always
After 8.0, filtering, filter cake is 8 hours dry at 100 DEG C for pH value control when change, rolls, extruded moulding.Deionized water is used at room temperature
Washing 5 times.Then wet bar is 10 hours dry at 80 DEG C, and 500 DEG C roast 4 hours, obtains catalyst F.Catalyst composition and main
Property is shown in Table 1.
Comparative example 3
According to method for preparing catalyst disclosed in CN201510212110.9, prepare identical with the catalyst of embodiment 1 composition
Reference agent G.Aluminium chloride, nickel chloride solution are added into dissolving tank 1, prepares working solution A, Ni is in terms of NiO in mixed solution A
Weight concentration is 28g/L, and Al is with Al2O3The weight concentration of meter is 19g/L.Into dissolving tank 2 be added aluminium chloride, ammonium metatungstate and
Ammonium molybdate prepares working solution B, and W is in mixed solution B with WO3The weight concentration of meter is 30g/L, and Mo is with MoO3Counting weight concentration is
36g/L, Al are with Al2O3The weight concentration of meter is 26g/L.It is that solution A, plastic temperature is added in 10wt% ammonium hydroxide under stiring by concentration
Degree is maintained at 60 DEG C, at the end of pH value control 7.8, gelation time control generated nickeliferous, aluminum precipitation object slurries I at 50 minutes.
500mL deionized water is added in reactor tank, is that 10wt% ammonium hydroxide and solution B cocurrent are added in reactor tank by concentration, gelling temperature
Be maintained at 60 DEG C, in cocurrent plastic reaction process pH value control 7.8, gelation time control at 2.0 hours, generate tungstenic, molybdenum,
Aluminum precipitation object slurries II.By it is above two containing sediment slurry mix after aging, ageing time 3.8 hours, 75 DEG C of aging temperature, always
At the end of change then pH value control is filtered, filter cake carries out hydro-thermal process, hydro-thermal process under the water vapour containing urea 7.8
Condition: the molar ratio of urea and active metal atom total amount is 3:1, and temperature is 230 DEG C, pressure 3.5MPa, and the processing time is 4
Hour, the material after hydro-thermal process is 8 hours dry at 100 DEG C, rolls, extruded moulding.It is washed with deionized at room temperature 5 times.
Then wet bar is 10 hours dry at 80 DEG C, and 500 DEG C roast 4 hours, obtains catalyst G.Catalyst composition and main character are shown in Table
1。
Comparative example 4
By method for preparing catalyst disclosed in CN102049265A, preparation and the catalyst of embodiment 1 form identical reference agent
H.Aluminium chloride, nickel chloride, ammonium metatungstate preparating acid sex work solution A are added into dissolving tank, takes 100g ammonium hydrogen carbonate to be made into and rubs
The solution that your concentration is 2.0mol/L.500mL water is added into reactor tank, temperature rises to 60 DEG C.It in the case of stirring, will be molten
Liquid A, ammonium bicarbonate aqueous solution and concentration be 10wt% ammonium hydroxide cocurrent be added reactor tank in plastic, 60 DEG C of gelling temperature, gelation time
3.0 hours, the pH value of plastic slurry was 7.8.Aging 3.8 hours after cemented into bundles, pH value is 8.0 at the end of aging.So
After filter, molybdenum trioxide is added in obtained filter cake, and mashing stirs evenly, and filters, and filter cake is 8 hours dry at 100 DEG C, rolls, and squeezes
Item molding.It is washed with deionized at room temperature 5 times.Then wet bar is 10 hours dry at 80 DEG C, and 500 DEG C roast 4 hours, is urged
Agent H.Catalyst composition and main character are shown in Table 1.
Embodiment 5
The present embodiment is WS in sulphided state catalyst2/MoS2The measurement of average platelet length and the average tap pile number of plies.To made
The TEM photo of standby bulk phase catalyst is statisticallyd analyze, and statistics area is greater than 20000nm2, the WS of statistics2/MoS2Lamella
Sum is more than 400.According to calculation formula (1) and (2) to bulk phase catalyst WS2/MoS2Lamella average length and average tap pile
The number of plies carries out statistics calculating, is as a result listed in table 3.
(1)
(2)
In formula (1), (2),L A For WS2/MoS2Lamella average length,L i For WS2/MoS2Lamella length, nm;n i It is for lengthL i 's
WS2/MoS2Piece number of layers,N A For WS2/MoS2The average tap number of plies;N i For WS2/MoS2The number of plies is accumulated,m i It is for the accumulation number of pliesN i
WS2/MoS2Piece number of layers.
Using catalyst A, B, C, D of the present invention and comparative example catalyst E, F, G, H, sulphur is carried out on adding hydrogen microreactor
Change, the admission space of catalyst is 10mL, vulcanizing agent CS2, sulfurized oil is hexamethylene, CS2Dosage be theory need sulfur content
110%.Presulfurization condition are as follows: temperature of reactor is 110 DEG C into sulfiding reagent, 320 DEG C of vulcanization reaction temperature, Hydrogen Vapor Pressure
6.0MPa, air speed 2.0h-1, time 10h.
Embodiment 6
The present embodiment is catalyst activity evaluation experimental of the present invention, and is compared with comparative example catalyst.It is urged using the present invention
Agent A, B, C, D and comparative example catalyst E, F, G, H, on 200mL small hydrogenation device carry out comparative evaluation's test, in order into
One step evaluates the ability of catalyst Deitrogenatin, therefore has selected the huge port catalytic diesel oil that nitrogen content is high, difficulty of processing is big former for test
Material, raw material main character are shown in Table 4.Catalyst activity evaluates process conditions: hydrogen partial pressure 6.4MPa, and reaction temperature is 360 DEG C, liquid
When volume space velocity be 2.0h-1, hydrogen to oil volume ratio 500:1, evaluation result is shown in Table 5.It is examined using gas chromatography-flame photometric detector
Sulfur compound and nitride type in device (GC-AED) detection hydrofined oil are surveyed, the results are shown in Table 6 and table 7.
As seen from Table 2, compared with comparative example catalyst, feelings that catalyst of the present invention does not change substantially in active metal amount
Under condition, MoS2/WS2The average tap number of plies increase, lamella average length reduces, and hydrogenation sites number increased significantly.From table
The evaluation result of 5-7 finds out that catalyst of the present invention has excellent hydrodenitrogenationactivity activity, is removing 1,8-DMCB and Isosorbide-5-Nitrae, 8-
High hydrogenation activity is shown when TMCB macromolecular nitride, is conducive to the hydrodesulfurization activity for improving catalyst.The present invention urges
Agent is for working process light fraction oil, when in particular for the big poor-quality diesel-oil by cut fraction of processing nitrogen content height, difficulty of processing,
With excellent ultra-deep hydrodesulfuration and nitrogen removal performance, and improve the Cetane number of diesel oil.
The catalyst composition and property of 1 embodiment of table and comparative example preparation
Catalyst number | A | B | C | D | E | F | G | H |
Ni, in terms of NiO, wt% | 19 | 24 | 20 | 18 | 19 | 19 | 19 | 19 |
W, with WO3Meter, wt% | 35 | 30 | 28 | 33 | 35 | 35 | 35 | 35 |
Mo, with MoO3Meter, wt% | 18 | 16 | 20 | 19 | 18 | 18 | 18 | 18 |
Al, with Al2O3Meter, wt% | Surplus | Surplus | Surplus | Surplus | Surplus | Surplus | Surplus | Surplus |
Other/wt% | - | ZrO2/4.0 | - | - | - | - | - | - |
Specific surface area, m2/g | 205 | 194 | 201 | 197 | 175 | 179 | 219 | 225 |
Kong Rong, mL/g | 0.310 | 0.297 | 0.303 | 0.301 | 0.271 | 0.273 | 0.325 | 0.334 |
Mechanical strength, N/mm | 16.8 | 17.5 | 17.1 | 17.4 | 16.7 | 17.2 | 15.8 | 14.7 |
The average tap number of plies and lamella average length of MoS2/WS2 in 2 bulk phase catalyst of table
Catalyst number | Average stacking number NA | Average length LA, nm |
A | 8.40 | 4.94 |
B | 8.22 | 4.98 |
C | 8.30 | 4.99 |
D | 8.26 | 5.02 |
E | 4.88 | 7.92 |
F | 5.03 | 8.01 |
G | 5.97 | 7. 85 |
H | 5.93 | 7. 62 |
The distribution of the accumulation number of plies and lamella length of MoS2/WS2 in 3 bulk phase catalyst of table
Catalyst number | A | B | C | D | E | F | G | H |
The distribution of the piece number of plies, % | | | | | | | | |
4.0 layers of < | 4.05 | 4.14 | 4.28 | 4.35 | 30.22 | 32.56 | 24.98 | 20.56 |
4.0 to less than 7.0 layers | 10.47 | 10.62 | 10.31 | 10.41 | 66.22 | 64.98 | 71.26 | 74.26 |
7.0 ~ 9.0 layers | 74.93 | 74.22 | 74.45 | 74.18 | 3.56 | 2.46 | 3.76 | 5.18 |
9.0 layers of > | 10.55 | 11.02 | 10.96 | 11.06 | - | - | - | - |
Distribution of lengths, % | | | | | | | | |
< 2.0nm | 5.28 | 5.35 | 5.26 | 5.19 | 1.19 | 1.23 | 1.09 | 1.54 |
2.0 to less than 4.0nm | 14.45 | 14.36 | 14.29 | 14.45 | 4.58 | 5.26 | 4.98 | 4.74 |
4.0~6.0nm | 74.28 | 73.51 | 73.71 | 73.63 | 8.27 | 8.56 | 8.69 | 8.19 |
Greater than 6.0 to 8.0nm | 5.16 | 5.85 | 5.66 | 5.77 | 65.17 | 64.21 | 65.59 | 66.58 |
> 8.0nm | 0.83 | 0.93 | 1.08 | 0.96 | 20.79 | 20.74 | 19.65 | 18.95 |
4 feedstock oil main character of table
Project | Analyze result |
Density (20 DEG C), g/cm3 | 0.9025 |
Boiling range range, DEG C | 162-375 |
S, μ g/g | 5026 |
N, μ g/g | 1024 |
5 catalyst activity evaluation result of table
Catalyst number | A | B | C | D |
It generates oil density (20 DEG C), g/cm3 | 0.8700 | 0.8702 | 0.8702 | 0.8701 |
Boiling range range, DEG C | 173-371 | 173-372 | 172-371 | 171-372 |
S, μ g/g | 8.3 | 8.6 | 8.8 | 8.4 |
N, μ g/g | 8.1 | 8.4 | 8.5 | 8.8 |
5 catalyst activity evaluation result of continued
Catalyst number | E | F | G | H |
It generates oil density (20 DEG C), g/cm3 | 0.8856 | 0.8883 | 0.8804 | 0.8812 |
Boiling range range, DEG C | 173-374 | 172-374 | 176-373 | 175-373 |
S, μ g/g | 265.6 | 260.2 | 217.5 | 228.6 |
N, μ g/g | 78.2 | 74.8 | 60.9 | 62.1 |
The content of different sulfide in 6 hydrofined oil of table
Catalyst number | A | B | C | D | E |
Sulfur content in hydrofined oil, μ g/g | 8.3 | 8.6 | 8.8 | 8.4 | 265.6 |
C1- DBT, μ g/g | 0 | 0 | 0 | 0 | 48.3 |
4- BMDBT, μ g/g | 1.9 | 2.0 | 2.1 | 1.8 | 69.2 |
6-BMDBT, μ g/g | 2.0 | 2.1 | 2.0 | 2.0 | 65.6 |
4,6- BMDBT, μ g/g | 4.4 | 4.5 | 4.7 | 4.6 | 82.5 |
Continued 6
Catalyst number | F | G | H |
Sulfur content in hydrofined oil, μ g/g | 260.2 | 217.5 | 228.6 |
C1- DBT, μ g/g | 40.7 | 33.4 | 37.8 |
4- BMDBT, μ g/g | 61.5 | 54.9 | 56.5 |
6-BMDBT, μ g/g | 68.4 | 56.3 | 60.3 |
4,6- BMDBT, μ g/g | 89.6 | 72.9 | 74.0 |
The content of different nitride in 7 hydrofined oil of table
Catalyst number | A | B | C | D | E |
Nitrogen content in hydrofined oil, μ g/g | 8.1 | 8.4 | 8.5 | 8.8 | 78.2 |
1- MCB, μ g/g | 1.5 | 1.6 | 1.5 | 1.7 | 28.3 |
1,8-BMCB, μ g/g | 2.2 | 2.0 | 2.1 | 2.1 | 34.9 |
Isosorbide-5-Nitrae, 8- TMCB, μ g/g | 4.4 | 4.8 | 4.9 | 5.0 | 15.0 |
Continued 7
Catalyst number | F | G | H |
Nitrogen content in hydrofined oil, μ g/g | 74.8 | 60.9 | 62.1 |
1-MCB, μ g/g | 24.2 | 18.1 | 17.8 |
1,8-BMCB, μ g/g | 35.3 | 28.3 | 29.5 |
Isosorbide-5-Nitrae, 8-TMCB, μ g/g | 15.3 | 14.5 | 14.8 |
Note: the main difficult de- nitrogenous compound of hydrodenitrogeneration is the carbazole (CB) that molecule is larger, has steric hindrance, 1- methyl carbazole
(1-MCB), 1,8- Dimethylcarbazole (1,8-BMCB), Isosorbide-5-Nitrae, 8- trimethyl carbazole (Isosorbide-5-Nitrae, 8-TMCB) etc..