CN103374402B - Hydro-upgrading method of catalytic cracking raw oil - Google Patents

Hydro-upgrading method of catalytic cracking raw oil Download PDF

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CN103374402B
CN103374402B CN201210107558.0A CN201210107558A CN103374402B CN 103374402 B CN103374402 B CN 103374402B CN 201210107558 A CN201210107558 A CN 201210107558A CN 103374402 B CN103374402 B CN 103374402B
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catalyst
content
described
nickel
characterized
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CN201210107558.0A
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CN103374402A (en
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胡大为
杨清河
刘佳
孙淑玲
聂红
王奎
李大东
戴立顺
刘学芬
邵志才
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中国石油化工股份有限公司
中国石油化工股份有限公司石油化工科学研究院
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Abstract

The invention provides a hydro-upgrading method of catalytic cracking raw oil. The method comprises the step of contacting the raw oil with a catalyst composition under the hydrotreating reaction condition, wherein the catalyst composition comprises a hydrodemetallization catalyst I, a hydrodemetallization catalyst II and a hydrodemetallization catalyst III; the catalysts in the catalyst composition are arranged in such a manner that the raw oil is sequentially in contact with the catalyst I, the catalyst II and the catalyst III; with the total quantity of the catalyst composition as the benchmark, the content of the catalyst I is 5-60% by volume, the content of the catalyst II is 10-70% by volume, and the content of the catalyst III is 5-60% by volume; the catalyst II contains a carrier, metal components including molybdenum, cobalt and nickel and auxiliary components selected from phosphorus and boron; with the catalyst II as the benchmark, the content of molybdenum is 5-20wt%, the total content of cobalt and nickel is 1-6wt% and the contents of the auxiliary components selected from phosphorus and boron are 0.5-5wt% by oxides; and the atomic ratio of cobalt to nickel is 2-4.

Description

A kind of hydrogenation modification method of catalytically cracked stock

Technical field

The present invention relates to the hydroprocessing process of hydrocarbon ils, particularly relate to a kind of method of by hydrotreatment, catalytically cracked stock being carried out to upgrading.

Background technology

By catalytic cracking process and catalysts influence, in order to improve light oil yield, reduce catalyst consumption, require that in heavy oil catalytic cracking raw material oil, W metal+V content should lower than 20ppm, sulphur content is lower than 0.5%, and carbon residue content is less than 6.0%.But along with the continuous aggravation of current crude oil heaviness, in poor quality trend, residual hydrocracking just requires to have higher impurity removal ability and reaction stability as fcc raw material preprocessing process.Improve impurity removal percentage to be realized by the severity deepening hydrotreatment reaction, but also can cause the shortening in catalyst runs life-span like this.Therefore new catalyzer and processing and treating method is adopted to be only the optimal selection of production high-quality catalytically cracked material.

Summary of the invention

The technical problem to be solved in the present invention is for prior art demand, provide a kind of newly, the method for by hydrotreatment, catalytically cracked stock being carried out to upgrading.

The present invention relates to following content:

1. the hydrogenation modification method of a catalytically cracked stock, comprise at hydrotreating reaction conditions, described stock oil is contacted with a kind of catalyst combination, described catalyst combination comprises Hydrodemetalation catalyst I, Hydrodemetalation catalyst II and Hydrobon catalyst III, in described catalyst combination the layout of each catalyzer make described stock oil successively with comprise catalyst I, catalyst I I contacts with catalyst I II, by volume and with the total amount of described catalyst combination for benchmark, the content of described catalyst I is 5-60%, the content of catalyst I I is 10-70%, the content of catalyst I II is 5-60%, wherein, described catalyst I I contains carrier, metal component molybdenum, cobalt and nickel, and be selected from the adjuvant component of phosphorus and boron, with oxide basis and with catalyst I I for benchmark, the content of described molybdenum is 5 ~ 20 % by weight, the content sum of cobalt and nickel is 1 ~ 6 % by weight, the content being selected from the adjuvant component of phosphorus and boron is 0.5-5 % by weight, wherein, the atomic ratio of cobalt and nickel is 2 ~ 4.

2, the method according to 1, is characterized in that, in described catalyst I I, the content of molybdenum is 8 ~ 15 % by weight, the content sum of cobalt and nickel is 1.5 ~ 4 % by weight, the content being selected from the adjuvant component of phosphorus and boron is 1 ~ 4 % by weight, and wherein, the atomic ratio of cobalt and nickel is 2.2 ~ 3.2.

3, the method according to 1 or 2, is characterized in that, in described catalyst I I, the content of nickel is less than 1.2%.

4, the method according to 3, is characterized in that, in described catalyst I I, the content of nickel is 0.5 ~ 1.1%.

5, the method according to 1, is characterized in that, by volume and with the total amount of described catalyst combination for benchmark, the content of the content of the catalyst I in described catalyst combination to be the content of 10-50%, catalyst I I be 20-60%, catalyst I II is 10-50%

6, method according to 1, it is characterized in that, described catalyst I comprises catalyst I a, described catalyst I a contains carrier, be selected from nickel and/or cobalt, the hydrogenation active metals component of molybdenum and/or tungsten, containing or not containing being selected from boron, phosphorus, one or more adjuvant components in fluorine, with catalyst I a for benchmark, with the content of the nickel of oxide basis and/or cobalt for 0.3-8 % by weight, the content of molybdenum and/or tungsten is 0.5-15 % by weight, boron is selected from element, phosphorus, the content of one or more adjuvant components in fluorine is 0 ~ 5 % by weight, wherein the pore volume of carrier is 0.6-1.4 ml/g, specific surface area is for being greater than 90 to being less than or equal to 350m 2/ g.

7, the method according to 6, is characterized in that, the pore volume of the carrier in described catalyst I a is 0.7-1.2 ml/g, and specific surface area is 100-200m 2/ g.

8, the method according to 6 or 7, is characterized in that, the support selected from alumina in described catalyst I a.

9, the method according to 8, is characterized in that, described aluminum oxide is the alumina supporter with double-hole.

10, the method according to 9, is characterized in that, described double-hole alumina supporter accounts for total pore volume 40-90% at the pore volume of aperture 10-30 nanometer, and aperture accounts for total pore volume 10-60% at the pore volume of 100-2000 nanometer.

11, the method according to 1, it is characterized in that, described catalyst I II contains the carrier being selected from aluminum oxide and/or silica-alumina, be selected from the hydrogenation active metals component of nickel and/or cobalt, molybdenum and/or tungsten, containing or not containing being selected from one or more adjuvant components in fluorine, boron and phosphorus, with catalyst I II for benchmark, be 1 ~ 5 % by weight with the content of the nickel of oxide basis and/or cobalt, the content of molybdenum and/or tungsten is 10 ~ 35 % by weight, is 0 ~ 9 % by weight in the content being selected from one or more adjuvant components in fluorine, boron and phosphorus of element.

12, the method according to 11, is characterized in that, the support selected from alumina in described catalyst I II.

13, the method according to 12, is characterized in that, the pore volume of described aluminum oxide is not less than 0.35 ml/g, and bore dia is that the pore volume in 40 ~ 100 dust holes accounts for more than 80% of total pore volume.

14, the method according to 6, is characterized in that, described catalyst I comprises and catalyst I athe catalyst I of layered arrangement b, by volume and with described catalyst I afor benchmark, catalyst I bcontent be less than 40%, described layering make described stock oil successively with catalyst I band catalyst I acontact, described catalyst I bcontaining carrier with optionally containing the hydrogenation active metals component being selected from group vib and group VIII, with oxide basis and with catalyst I bfor benchmark, the content of the metal component of described group vib is 0 to being less than or equal to 10 % by weight, and the content of the metal component of described group VIII is 0 to being less than or equal to 4 % by weight.

15, the method according to 14, is characterized in that, described catalyst I bcarrier contain 0-aluminum oxide, with mercury penetration method characterize, the pore volume of described carrier is 0.5-0.75ml/g, and specific surface area is 2-20m 2/ g.

16, the method according to 15, is characterized in that, described catalyst I bthe pore volume of carrier be 0.52-0.73ml/g, specific surface area is 5-16m 2/ g, there are two peaks at 45-1000 μm and 0.2-1mm in pore distribution curve.

17, the method according to 16, is characterized in that, described catalyst I bthe pore distribution curve of carrier there are two peaks at 45-100 μm and 0.2-1mm.

18, the method according to 14, is characterized in that, by volume and with described catalyst I afor benchmark, catalyst I bcontent be 5-30%.

19, the method according to 1, is characterized in that, the reaction conditions of described hydrotreatment reaction is: hydrogen dividing potential drop 6-20MPa, temperature is 300-450 DEG C, and during liquid, volume space velocity is 0.1-1h -1, hydrogen to oil volume ratio is 600-1500.

20, the method according to 19, is characterized in that, the reaction conditions of described hydrotreatment reaction is: hydrogen dividing potential drop is 10-18MPa, and temperature is 350-420 DEG C, and during liquid, volume space velocity is 0.2-0.6h -1, hydrogen to oil volume ratio is 800-1100.

According to method provided by the invention, wherein, the carrier of described catalyst I I can be the carrier that in prior art, any one is suitable for preparing heavy oil hydrogenating treatment catalyst, and they can be that commercially available commodity also can adopt arbitrary prior art to prepare.This kind of carrier has following physico-chemical property usually, comprising: pore volume is 0.5-1.0 ml/g, and be preferably 0.6-0.9 ml/g, specific surface is 160-400 rice 2/ gram, be preferably 180-350 rice 2/ gram.Preferred alumina supporter wherein.

The preparation method of described catalyst I I is included on carrier and introduces metal component molybdenum, cobalt and nickel, and be selected from the adjuvant component of phosphorus and boron, with oxide basis and with the total amount of catalyzer for benchmark, the introduction volume of each component makes the content of molybdenum in final catalyzer be 5 ~ 20 % by weight, be preferably 8 ~ 15 % by weight, the content sum of cobalt and nickel is 1 ~ 6 % by weight, be preferably 1.5 ~ 4 % by weight, the content being selected from the adjuvant component of phosphorus and boron is 0.5-5 % by weight, be preferably 1 ~ 4%, the atomic ratio of described cobalt and nickel is 2 ~ 4, is preferably 2.2 ~ 3.2.In further preferred embodiment, with oxide basis and with the total amount of catalyzer for benchmark, the introduction volume of described nickel is less than 1.2%, is more preferably 0.5 ~ 1.1%.

The described method introducing metal component on carrier can be prepare the usual method of hydrogenation catalyst, such as, adopt the method for dipping.Steeping process can adopt total immersion also can step impregnation.Namely adopt containing molybdenum, nickel and cobalt metal component and phosphorus or boron the method for solution impregnating carrier of compound introduce.This dipping can be by the solution impregnation containing a component composition preparation, also can be flood with the mixing solutions containing two or more component composition.By contained containing the concentration of each component composition and the consumption of steeping fluid in adjustment dipping, art technology easily realizes controlling the content of each component introducing catalyzer, does not repeat here.

The step of drying, roasting or not roasting is also comprised after described dipping.The method of described drying and roasting and condition are the conventional method and condition that catalyst preparing adopts.Such as, the condition of described drying comprises: drying temperature is 60 ~ 150 DEG C, and time of drying is 1 ~ 5 hour, and preferred drying temperature is 80 ~ 120 DEG C, and time of drying is 2 ~ 4 hours; Described roasting condition comprises: maturing temperature is 350-550 DEG C, and roasting time is 1-6 hour, and preferred maturing temperature is 400 ~ 500 DEG C, and roasting time is 2 ~ 4 hours.

The described compound containing molybdenum component is selected from one or more in its soluble compound, as one or more in molybdenum oxide, molybdate, paramolybdate, and preferably molybdenum oxide, ammonium molybdate, ammonium paramolybdate wherein.

Described nickeliferous and be selected from one or more in their soluble compound containing the compound of cobalt metal component, as one or more in the soluble complexes of Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, Cobaltous diacetate, cobaltous dihydroxycarbonate, cobalt chloride and cobalt, be preferably Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, cobaltous dihydroxycarbonate; One or more in the soluble complexes of nickelous nitrate, nickel acetate, basic nickel carbonate, nickelous chloride and nickel, are preferably nickelous nitrate, basic nickel carbonate.

Described P contained compound is selected from one or more in their soluble compound, as one or more in phosphoric acid, ammonium phosphate, ammonium hydrogen phosphate, primary ammonium phosphate, phosphoric acid salt, is preferably phosphoric acid and ammonium phosphate salt.

Described boron-containing compound is selected from one or more in their soluble compound, as one or more in boric acid, ammonium borate, ammonium biborate, borate, is preferably boric acid and ammonium borate salt.

According to catalyst I I of the present invention, can also the invention provides containing any impact the material that catalyst performance maybe can improve the catalytic performance of catalyzer provided by the invention.Such as, can containing components such as alkaline-earth metal, be benchmark with oxide basis and with catalyzer, the content of said components is no more than 10 % by weight, is preferably 0.5-5 % by weight.

When also containing the components such as alkaline-earth metal in described catalyzer, the introducing method of the components such as described alkaline-earth metal can be arbitrary method, to prepare the alumina supporter of alkaline including earth metal, the introducing method of the components such as described alkaline-earth metal can be the compound containing components such as described alkaline-earth metal is directly mixed with described pseudo-boehmite, shaping and roasting; Can be that the compound containing components such as described alkaline-earth metal and the compound containing other components are mixed with mixing solutions, afterwards with carrier described in this solution impregnation; Can also be by independent for the compound containing components such as alkaline-earth metal obtain solution, afterwards respectively with carrier described in these solution impregnation.When the components such as alkaline-earth metal and other organize introduce described carrier respectively time, preferably first use carrier described in the solution impregnation containing component composition such as described alkaline-earth metal and roasting, afterwards again by the solution impregnation of the compound containing other components, described maturing temperature is 250-600 DEG C, be preferably 350-500 DEG C, roasting time is 2-8 hour, is preferably 3-6 hour.

According to method provided by the invention, wherein, the effect that described catalyst I comprises catalyst I a is to be reacted by the hydrotreatment at this catalyzer, removes the macromole species such as the metal in raw material, bituminous matter and colloid.Therefore, wherein said catalyst I can be selected from prior art one or more that can realize arbitrarily in the catalyzer of this function.Such as, one or more in the hydrogenation protecting catalyst of mink cell focus processing, Hydrodemetalation catalyst are usually used in.They can be commercially available commodity or adopt any existing method preparation.

This type of catalyzer is usually containing heat-resistant inorganic oxide carrier and load hydrogenation active metals component on this carrier.Wherein, described heat-resistant inorganic oxide carrier is selected from one or more in the various heat-resistant inorganic oxides being commonly used for support of the catalyst and/or matrix.Such as, one or more in optional self-alumina, silicon oxide, titanium oxide, magnesium oxide, silica-alumina, alumina-silica magnesium, silica-magnesias, silica-zirconia, silica-alumina-titania, silicaalumina-magnesia, are preferably aluminum oxide.Described hydrogenation active component is selected from molybdenum and or tungsten, nickel and or cobalt.

Such as, a kind of catalyzer disclosed in ZL200310117322.6, this catalyzer contains a kind of macropore alumina supporter and load molybdenum on this carrier and/or tungsten and cobalt and/or nickel, be benchmark with oxide basis and with catalyzer, described catalyzer contains the carrier of the molybdenum of 0.5-15 % by weight and/or tungsten, the cobalt of 0.3-8 % by weight and/or nickel, equal amount, and it is characterized in that, described carrier contains a kind of halogen, with carrier total amount for benchmark, this carrier contains the aluminum oxide of 95-99 % by weight.

ZL200410037670.7 disclose a kind of there is double-hole alumina supporter and load molybdenum on this carrier and/or tungsten and cobalt and/or nickel, be benchmark with oxide basis and with catalyzer, described catalyzer contains the carrier of the molybdenum of 0.5-15 % by weight and/or tungsten, the cobalt of 0.3-8 % by weight and/or nickel, equal amount.

ZL200410096309.1 discloses a kind of residuum hydrogenating and metal-eliminating catalyst, this catalyzer contains a kind of Bimodal-pore alumina support and load molybdenum on this carrier and/or tungsten and nickel and/or cobalt metal component, the pore volume of wherein said Bimodal-pore alumina support is 0.8-1.6 ml/g, and specific surface area is 150-350m 2/ g, aperture accounts for total pore volume 40 ~ 90% at the pore volume of 10 ~ 30 nanometers, and aperture accounts for total pore volume 10 ~ 60% at the pore volume of 100 ~ 2000 nanometers.

ZL200510115349.0 discloses a kind of Hydrogenation active protective agent and preparation method thereof; this protective material contains alumina supporter, the load hydrogenation active metals component of significant quantity and halogen on this carrier; it is benchmark in element and with catalyzer; the content of described halogen is 0.5-10 % by weight, and the specific surface area of described carrier is 2-50m 2/ g, pore volume 0.4-1.2 ml/g, the precursor of one or more aluminum oxide and/or aluminum oxide and the halogen-containing compound of at least one, the shaping and method of roasting are prepared by comprising by described carrier.

These catalyzer all can be selected as described catalyst I for the present invention.About the more detailed preparation method of above-mentioned catalyzer, all on the books in above-mentioned patent documentation, in the lump their parts as content of the present invention are quoted here.

According to method provided by the invention, wherein, the predictive role of catalyst I II is the macromolecular cpds such as saturated polycyclic aromatic hydrocarbons, the wherein more difficult impurity such as sulphur, nitrogen removed is removed further, removes the carbon residue in stock oil simultaneously.Therefore, described catalyst I II can be selected from one or more that can realize in the catalyzer of this function any of the prior art.Such as, one or more in the Hydrobon catalyst that arbitrary prior art provides are selected from.They can be commercially available commodity or adopt any existing method preparation.

This type of catalyzer is usually containing heat-resistant inorganic oxide carrier, hydrogenation active metals component.Wherein, described heat-resistant inorganic oxide carrier is selected from one or more in the various heat-resistant inorganic oxides being commonly used for support of the catalyst and/or matrix.Such as, one or more in optional self-alumina, silicon oxide, titanium oxide, magnesium oxide, silica-alumina, alumina-silica magnesium, silica-magnesias, silica-zirconia, silica-titania, are preferably aluminum oxide.Described hydrogenation active metals component is nickel and or cobalt, tungsten and or molybdenum.The example of this kind of catalyzer as:

A kind of Hydrobon catalyst disclosed in ZL97112397.7, it consists of the heavy % of nickel oxide 1 ~ 5, the heavy % of Tungsten oxide 99.999 12 ~ 35, the heavy % of fluorine 1 ~ 9, all the other are aluminum oxide, this aluminum oxide be by one or more little porous aluminum oxides and one or more macroporous aluminium oxides according to 75: 25 ~ 50: 50 weight ratio be composited, wherein little porous aluminum oxide is the aluminum oxide that pore volume that bore dia is less than 80 dust holes accounts for total pore volume more than 95%, and macroporous aluminium oxide is the aluminum oxide that the pore volume in bore dia 60 ~ 600 dust hole accounts for total pore volume more than 70%.

ZL00802168.6 discloses a kind of Hydrobon catalyst, and this catalyzer contains at least one VI B race's metal on this alumina supporter of a kind of alumina supporter and load and/or at least one group VIII metal.The pore volume of described alumina supporter is not less than 0.35 ml/g, and bore dia is that the pore volume in 40 ~ 100 dust holes accounts for more than 80% of total pore volume, and it adopts special method preparation.

ZL200310117323.0 discloses a kind of Hydrobon catalyst, this catalyzer contains a kind of alumina supporter and load molybdenum on this carrier, nickel and tungsten metal component, be benchmark with oxide basis and with catalyzer, described catalyzer contains the molybdenum of 0.5-10 % by weight, the nickel of 1-10 % by weight, the tungsten of 12-35 % by weight and the carrier of equal amount, the preparation method of described catalyzer comprises and uses the solution of molybdate compound and nickeliferous successively, the solution impregnation of alumina carrier of tungsten compound, wherein said alumina supporter carries out drying after by the solution impregnation of molybdate compound, with nickeliferous, drying and roasting is carried out after the solution impregnation of tungsten compound, drying temperature is 100-300 DEG C, time of drying is 1-12 hour, maturing temperature is 320-500 DEG C, roasting time is 1-10 hour.

These catalyzer all can be used as described catalyst I II for the present invention.About the more detailed preparation method of above-mentioned catalyzer, all on the books in above-mentioned patent documentation, in the lump their parts as content of the present invention are quoted here.

Contriver finds further; when described catalyst I is the combination comprising Ib and Ia, the catalyst combination comprising hydrogenation activity guard catalyst I, Hydrodemetalation catalyst II and hydrotreating catalyst III described in can improving further adds the performance in man-hour for described stock oil.

Particularly, described catalyst I bfor a kind of containing or containing hydrogenation active metals, there is low specific surface area and the forming composition of large pore volume, further preferably the pore distribution curve of this forming composition is that micron order (or grade) is in bimodal distribution at bore dia.In a preferred embodiment, the preparation method of described carrier comprises:

(1) by hydrated aluminum oxide, can the organic additive of burn off, acid or alkali and water mixing, carry out drying, fragmentation afterwards and sieve, obtaining 20-60 object particle;

(2) particle step (1) obtained carries out mixing with Alumina gel and/or hydrated alumina slurry and shaping, carries out drying and roasting afterwards;

Wherein, hydrated aluminum oxide described in step (1), can the organic additive of burn off, and the ratio of mixture of acid or alkali and water is 100: 0.5-6: 0.5-10: 30-80; The particle obtained by step (1) in described step (2) with in the Mixing ratio by weight of the Alumina gel of aluminum oxide and/or hydrated alumina slurry for 100: 5-45; Described drying conditions comprises: temperature is 100-140 DEG C, and the time is 1-10 hour; Described roasting condition comprises: temperature is 1100-1540 DEG C, and the time is 1-10 hour.

Preferably wherein, hydrated aluminum oxide described in step (1), can the organic additive of burn off, acid or alkali and water ratio of mixture be 100: 0.6-3: 0.6-5: 35-75; The particle obtained by step (1) in described step (2) with in the Mixing ratio by weight of the Alumina gel of aluminum oxide and/or hydrated alumina slurry for 100: 5-40; Described drying conditions comprises: temperature is 110-130 DEG C, and the time is 2-8 hour; Described roasting condition comprises: temperature is 1200-1500 DEG C, and the time is 2-8 hour.Described can the organic additive of burn off be selected from starch, Mierocrystalline cellulose, polynary alcohol and carboxylic acid one or more, one or more in preferred starch, Mierocrystalline cellulose and polyvalent alcohol.

Optionally, introducing can also be comprised in described step (1) or (2) and be selected from siliceous, phosphorus, the step of the compound of one or more adjuvant components in alkali or alkaline-earth metal, be benchmark with oxide basis and with carrier, the introduction volume of the described compound containing adjuvant component, make the content of adjuvant component described in final carrier be no more than 25 % by weight, be preferably 1-20 % by weight.Described silicon-containing compound is selected from silicon sol, and P contained compound is selected from aluminium dihydrogen phosphate, and alkali metal-containing compound is selected from alkali-metal oxyhydroxide, and alkaline including earth metal compound is selected from oxide compound or the oxyhydroxide of alkaline-earth metal.

Here, described pore distribution curve refers to the velocity of variation (ordinate zou be dV/dlogD, X-coordinate be bore dia D (logD)) of pore volume (pore volume) with bore dia.

Wherein, the described hydrated aluminum oxide in the preparation method of described carrier is selected from the mixture of one or more among hibbsite, monohydrate alumina (comprising pseudo-boehmite) and amorphous hydroted alumina.Described acid can be any compound reacted acid in water medium, and such as, they can be formic acid, acetic acid, propionic acid, sulfuric acid, nitric acid, hydrochloric acid, oxalic acid, silicofluoric acid, hydrofluoric acid, preferably nitric acid, hydrochloric acid, sulfuric acid wherein; Described alkali can be the compound of any react acid in water medium, such as, they can be ammonia, ammoniacal liquor, alkali-metal oxyhydroxide (as sodium hydroxide, potassium hydroxide, magnesium hydroxide), alkali-metal carbonate (as salt of wormwood, Quilonum Retard, sodium carbonate, saleratus, calcium carbonate, magnesiumcarbonate, barium carbonate), preferably salt of wormwood, Quilonum Retard wherein.

Be enough to make described hydrated aluminum oxide, can the organic additive of burn off, acid or alkali and water fully mix, under obtaining the prerequisite of 20-60 object particulate matter after this mixture drying, fragmentation, the present invention to realizing this mixing in step (1), broken mode does not limit.Such as, can be in banded extruder first by hydrated aluminum oxide with can the organic additive of burn off mix, acid or alkali are mixed with water, afterwards, the mixing of materials in the mixing solutions of acid or alkali and water and banded extruder are extruded, extrudate drying, fragmentation and sieve.Mixing in step (2) is to meet premised on shaping requirement, and described shaping method can be carried out according to a conventional method, such as, can be compressing tablet, spin, extrusion moulding etc.For the needs of satisfied different forming method, comprise introducing in moulding process and help forming agent, such as, introduce appropriate water, peptizing agent (as one or more being selected from nitric acid, acetic acid and citric acid), extrusion aid (as being one or more in sesbania powder, Mierocrystalline cellulose), described the help consumption of forming agent and adjustment thereof are well known to those skilled in the art, and are not repeated herein.

When described catalyst I b contains hydrogenation active metals component, the step introducing hydrogenation active metals component in described forming composition is included in the preparation method of this catalyzer, the method introducing hydrogenation active component is preferably pickling process, comprise preparation contain the solution of the compound of hydrogenation active metals and use this solution impregnating carrier, carry out drying afterwards, roasting or not roasting, described hydrogenation active metals component is selected from the metal component of group vib and the metal component of group VIII, be benchmark with oxide basis and with catalyzer, the described compound containing hydrogenation active metals makes the content of the metal component of the group vib in final catalyzer be greater than 0 to being less than or equal to 10 % by weight in the concentration of described solution and the consumption of described solution, the content of the metal component of described group VIII is greater than 0 to being less than or equal to 4 % by weight, described drying conditions comprises: temperature is 100-250 DEG C, and the time is 1-10 hour, described roasting condition comprises: temperature is 360-500 DEG C, and the time is 1-10 hour.Preferably, the metal component of described group vib is selected from molybdenum and/or tungsten, the metal component of group VIII is selected from cobalt and/or nickel, be benchmark with oxide basis and with catalyzer, the described compound containing hydrogenation active metals makes the content of the metal component of the group vib in final catalyzer be 3-6 % by weight in the concentration of described solution and the consumption of described solution, and the content of the metal component of group VIII is 1-3 % by weight; Described drying conditions comprises: temperature is 100-140 DEG C, and the time is 1-6 hour; Described roasting condition comprises: temperature is 360-450 DEG C, and the time is 2-6 hour.

Wherein, the described compound containing group vib metal is selected from one or more in the soluble compound of these metals, such as, can be one or more in silicotungstic acid, silicotungstate, phospho-molybdic acid, phosphomolybdate, molybdate, paramolybdate, tungstate, metatungstate, ethyl metatungstate.

The described compound containing group VIII metal is selected from one or more in the soluble compound of these metals, such as, is selected from one or more in their nitrate, carbonate, subcarbonate, hypophosphite, phosphoric acid salt, vitriol, muriate.

According to method provided by the invention; the described catalyst combination comprising hydrogenation activity guard catalyst I, Hydrodemetalation catalyst II and hydrotreating catalyst III can layering fill in same reactor successively, also can be to use in the reactor filling in several series connection successively.Be enough to make described stock oil successively with comprise prerequisite that hydrogenation activity guard catalyst I, Hydrodemetalation catalyst II contact with hydrotreating catalyst III under, this present invention is not particularly limited.

The present invention is owing to adopting a kind of catalyst combination with over-all propertieies such as fine better demetalization, desulfurization and de-carbon residues, be particularly suitable for the hydrotreatment of one or more stock oils be selected from vacuum residuum, deep drawing wax oil, frivolous asphalt oil, heavy deasphalted oil, wax tailings etc., can be catalytic cracking unit and stock oil through hydro-upgrading is provided.

According to after the hydrotreatment that described method obtains oil metal content be 20 below μ g/g, sulphur content less than 0.5%, carbon residue content is less than 6.0%.

Embodiment

The present invention is described further for the following examples.

Agents useful for same in example, except as expressly described, is chemically pure reagent.

Embodiment 1-4 illustrates and the invention provides method catalyst I I and preparation thereof.

The carrier of Kaolinite Preparation of Catalyst II and preparation thereof:

Carrier Z1 and preparation thereof:

The sesbania powder of pseudo-boehmite dry glue powder RPB110 and 10 gram that 300 grams of Chang Ling catalyst plants are produced is mixed, be at room temperature the aqueous nitric acid of 1% by the concentration of this mixture and 360 milliliters, mix, it is after plastic that double screw banded extruder continues kneading, be extruded into the trilobal bar of ф 1.5 millimeters, wet bar after 3 hours, 3 hour obtains carrier Z1 in 700 DEG C of roastings through 120 DEG C of dryings.Measure the specific surface of Z1, pore volume and pore size distribution, the results are shown in Table 1.

Carrier Z2 and preparation thereof:

Pseudo-boehmite dry glue powder by the pseudo-boehmite dry glue powder RPB90 that 300 grams of Chang Ling catalyst plants are produced) and 10 grams of sesbania powder mix, add the aqueous nitric acid that 330 ml concns are 1%, mix, it is after plastic that double screw banded extruder continues kneading, be extruded into the butterfly bar of ф 1.1 millimeters, wet bar after 2 hours, 4 hour obtains carrier Z2 in 600 DEG C of roastings through 110 DEG C of dryings.Measure the specific surface of Z2, pore volume and pore size distribution, result is as shown in table 1.

Table 1

Carrier specific surface, pore volume and pore size distribution adopt B E T Brunauer Emett Teller method of nitrogen adsorption at low temperature to measure.

Embodiment 1

Get 200 grams of Z1, with 500 milliliters containing MoO 3120 grams per liters, NiO 8 grams per liter, CoO 20 grams per liter, B 2o 3the ammonium molybdate of 15 grams per liters, nickelous nitrate, Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES and boric acid mixing solutions flood 1 hour, dry 2 hours after filtration in 120 DEG C, and 450 DEG C of roastings 4 hours, obtain catalyst I I1.With the gross weight of catalyzer for benchmark, adopt molybdenum oxide, cobalt oxide, nickel oxide and the B in Xray fluorescence spectrometer mensuration catalyst I I1 2o 3content, measurement result is as shown in table 2.(all appts is Rigaku electric machine industry Co., Ltd. 3271 type Xray fluorescence spectrometer, and concrete grammar is shown in Petrochemical Engineering Analysis method RIPP133-90)

Embodiment 2

Get 200 grams of Z2, with 220 milliliters containing MoO 3172 grams per liters, NiO 9 grams per liter, CoO 32 grams per liter, P 2o 5the molybdenum oxide of 43 grams per liters, basic nickel carbonate, cobaltous dihydroxycarbonate and phosphoric acid mixing solutions flood 2 hours, dry 2 hours in 120 DEG C, and 550 DEG C of roastings 2 hours, obtain catalyst I I2.The molybdenum oxide in catalyst I I2, cobalt oxide, nickel oxide and P is measured according to the mode identical with embodiment 1 2o 5content, result is as shown in table 2.

Embodiment 3

Get 200 grams of Z2, with 200 milliliters containing MoO 3122 grams per liters, NiO 9 grams per liter, CoO 18 grams per liter, P 2o 5the molybdenum oxide of 35 grams per liters, basic nickel carbonate, cobaltous dihydroxycarbonate and phosphoric acid mixing solutions flood 1 hour, dry 2 hours in 120 DEG C, and 480 DEG C of roastings 4 hours, obtain catalyst I I3.The molybdenum oxide in catalyst I I3, nickel oxide and cobalt oxide, P is measured according to the mode identical with embodiment 1 2o 5content, result is as shown in table 2.

Embodiment 4

Get 200 grams of Z1, with 500 milliliters containing CoO 12 grams per liter, B 2o 3jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, the boric acid mixing solutions of 9 grams per liters flood 1 hour, dry 3 hours after filtration in 110 DEG C, and 350 DEG C of roastings 2 hours contain MoO with 200 milliliters 392 grams per liters, molybdenum oxide, the basic nickel carbonate mixing solutions of NiO 7 grams per liter flood 1 hour, dry 2 hours in 120 DEG C, and 480 DEG C of roastings 4 hours, obtain catalyst I I4.The molybdenum oxide in catalyst I I4, nickel oxide and cobalt oxide, B is measured according to the mode identical with embodiment 1 2o 3content, result is as shown in table 2.

Comparative example 1

Get 200 grams of Z1, with 500 milliliters containing MoO 3120 grams per liters, ammonium molybdate and the nickelous nitrate mixing solutions of NiO 28 grams per liter flood 1 hour, dry 2 hours after filtration in 120 DEG C, and 450 DEG C of roastings 4 hours, obtain catalyzer DII1.Measure the content of molybdenum oxide in catalyzer DII1 and nickel oxide according to the mode identical with embodiment 1, result is as shown in table 2.

Comparative example 2

Get 200 grams of Z2, with 500 milliliters containing MoO 3135 grams per liters, NiO 12 grams per liter, the ammonium molybdate of CoO 20 grams per liter, nickelous nitrate, Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES mixing solutions flood 1 hour, dry 2 hours after filtration in 120 DEG C, and 450 DEG C of roastings 4 hours, obtain catalyzer DII2.With the gross weight of catalyzer for benchmark, adopt the content of the molybdenum oxide in Xray fluorescence spectrometer mensuration catalyzer DII2, cobalt oxide, nickel oxide, measurement result is as shown in table 2.(all appts is Rigaku electric machine industry Co., Ltd. 3271 type Xray fluorescence spectrometer, and concrete grammar is shown in Petrochemical Engineering Analysis method RIPP133-90)

Table 2

Embodiment 5-8

Embodiment 5-8 illustrates application and the performance thereof of catalyst I I provided by the invention.

With nickel content be 29ppm, content of vanadium is 83ppm, sulphur content is 4.7%, carbon residue be the long residuum of 15% nitrogen content 0.3% for raw material, evaluate catalysts on 100 milliliters of small fixed reactors.

Respectively catalyst I I 1, II 2, II 3, II 4 are broken into the particle of diameter 2-3 millimeter, catalyzer loading amount is 100 milliliters.Reaction conditions is: when temperature of reaction 380 DEG C, hydrogen dividing potential drop 14 MPa, feeding liquid, volume space velocity is 0.6 hour -1, hydrogen to oil volume ratio is 1000, reacts after 200 hours and samples, the content of nickel and vanadium in the oil after adopting inductive coupling plasma emission spectrograph (ICP-AES) to measure process.(instrument is U.S. PE company PE-5300 type plasma quantometer, and concrete grammar is shown in Petrochemical Engineering Analysis method RIPP124-90)

Coulometry is used to measure the content (concrete grammar is shown in Petrochemical Engineering Analysis method RIPP62-90) of sulphur.

Coulometry is used to measure the content (concrete grammar is shown in Petrochemical Engineering Analysis method RIPP63-90) of nitrogen.

Use microdetermination carbon residue content (concrete grammar is shown in Petrochemical Engineering Analysis method RIPP148-90).

Calculate the decreasing ratio of sulphur, carbon residue, nitrogen and metal according to the following formula respectively:

The results are shown in Table 3.

Comparative example 3-4

According to every impurity removal performance of method evaluation catalyzer DII1, DII2 of embodiment 5-8, the results are shown in Table 3.

Table 3

Can be seen there is obvious lifting by the overall impurity removal specific activity prior art that the invention provides catalyzer by table 3 result, especially promote more remarkable in desulfurization and de-carbon residue.

Embodiment 9-13 illustrates and the invention provides method hydrogenation protecting catalyst Ib and preparation thereof.

Embodiment 9

By 100 grams of pseudo-boehmites (Chang Ling catalyst plant produce, butt is 65 % by weight), 3 grams of sesbania powder and 155 grams containing 1.5% nitre aqueous acid.Kneading in double screw banded extruder is also extruded with the cylindrical orifice plate of φ 2.0mm, and dry bar, in 120 DEG C of dryings 4 hours, is pulverized and sieves by wet bar.

Get 40 grams of aforementioned screenings and obtain 40-60 object particulate matter, it is mixed with 10 grams of pseudo-boehmites and 1.2 grams of magnesium oxide, add 5 grams, water and 15 grams of silicon sol (Qingdao Jian Hui silica gel company limiteds in the mixture, dioxide-containing silica 29%) and shaping according to roller forming method, and obtaining particle diameter is 5.5-6.5mm spheroidal particle.Afterwards, by this particle in 120 DEG C of dryings 4 hours, 1200 DEG C of roastings 3 hours, obtain hydrogenation protecting catalyst Ib-1 (Z9).

X-ray diffraction is adopted to characterize, catalyst I b-1 has Alpha-alumina structure, adopting pressure mercury method to characterize, there are two peaks at 45-1000 μm and 0.2-1mm in catalyst I b-1 pore distribution curve, and its pore volume, specific surface area and pore distribution value and catalyst I b-1 composition list in table 4.

Embodiment 10

By 100 grams of pseudo-boehmites (Chang Ling catalyst plant produce, butt is 65 % by weight), 3 grams of sesbania powder and 155 grams containing the aqueous solution of 1.5% nitric acid and 0.5% salt of wormwood.Kneading in double screw banded extruder is also extruded with the cylindrical orifice plate of φ 2.0mm, and dry bar, in 120 DEG C of dryings 4 hours, is pulverized and sieves by wet bar.The rear sieve of pulverizing is got 40-60 mesh sieve and is divided.

Get aforementioned screening to obtain 40-60 object particulate matter 45g and mix with 5g pseudo-boehmite, add water 8g, (Yueyang is polymerized to Chemical Co., Ltd. to Alumina gel, solid content: after 25%) 20g and aluminium dihydrogen phosphate (Chinese and Western, Beijing tech science and technology limited Company) 2.1g mixes with aforementioned screening, extruded moulding.Shaping rear pelletizing, shaping, by bead after shaping 120 DEG C of dryings 4 hours, 1400 DEG C of roastings 3 hours, obtains carrier Z10.

Adopt X-ray diffraction to characterize, carrier Z10 has Alpha-alumina structure, and adopt pressure mercury method to characterize, carrier Z10 pore distribution curve occurs two peaks at 45-1000 μm and 0.2-1mm, its pore volume, specific surface area and pore distribution value and vehicle group in column in table 4.

Get carrier 20 grams of Z10, in saturated leaching mode with containing 1.42g ammonium molybdate (containing MoO 382%) and the solution 15.5 milliliters dipping of 1.3g nickelous nitrate (containing NiO 25%), 120 DEG C of dryings 4 hours after dipping, 420 DEG C of roastings 3 hours guard catalyst Ib-2 of the present invention.The content adopting X-fluorescence method to measure hydrogenation active metals component in catalyzer lists in table 5.

Embodiment 11

By 100 grams of pseudo-boehmites (Chang Ling catalyst plant produce, butt is 65 % by weight), 3 grams of sesbania powder and 155 grams containing the aqueous solution of 1.5% nitric acid and 0.5% Quilonum Retard.Kneading in double screw banded extruder is also extruded with the cylindrical orifice plate of φ 5.0mm, and dry bar, in 120 DEG C of dryings 4 hours, is pulverized and sieves by wet bar.

Take 20-40 object screening 42g and 8g pseudo-boehmite to mix, take 25g Alumina gel (Yueyang is polymerized to Chemical Co., Ltd., solid content: 25%), after mixing, extruded moulding.Shaping rear pelletizing, shaping, by bead after shaping 120 DEG C of dryings 4 hours, 1100 DEG C of roastings 3 hours, obtains carrier Z11.

Adopt X-ray diffraction to characterize, carrier Z11 has Alpha-alumina structure, and adopt pressure mercury method to characterize, carrier Z11 pore distribution curve occurs two peaks at 45-1000 μm and 0.2-1mm, its pore volume, specific surface area and pore distribution value and vehicle group in column in table 4.

Get carrier 30 as one kind gram Z11, in saturated leaching mode with containing 2.2g ammonium molybdate (containing MoO 382%) and the solution 25 milliliters dipping of 2.0g nickelous nitrate (containing NiO25%), 120 DEG C of dryings 4 hours after dipping, 420 DEG C of roastings 3 hours guard catalyst Ib-3 of the present invention.The content adopting X-fluorescence method to measure hydrogenation active metals component in catalyzer lists in table 5.

Embodiment 12

By 100 grams of pseudo-boehmites (Chang Ling catalyst plant produce, butt is 65 % by weight), 3 grams of sesbania powder and 155 grams containing 1.8% nitre aqueous acid.Kneading in double screw banded extruder is also extruded with the cylindrical orifice plate of φ 5.0mm, and dry bar, in 120 DEG C of dryings 4 hours, is pulverized and sieves by wet bar.

Take 20-40 object screening 20g and 40-60 object screening 15g, mix with 15g pseudo-boehmite, take 25g silicon sol (Qingdao Jian Hui silica gel company limited, dioxide-containing silica 29%), mix with aforementioned screening, extruded moulding.Shaping rear pelletizing, shaping, by bead after shaping 120 DEG C of dryings 4 hours, 1400 DEG C of roastings 3 hours, obtains carrier Z12.

Adopt X-ray diffraction to characterize, carrier Z12 has Alpha-alumina structure, and adopt pressure mercury method to characterize, carrier Z12 pore distribution curve occurs two peaks at 45-1000 μm and 0.2-1mm, its pore volume, specific surface area and pore distribution value and vehicle group in column in table 4.

Get carrier 20 grams of Z12, in saturated leaching mode with containing 0.86g ammonium molybdate (containing MoO 382%) and the solution 13 milliliters dipping of 1.25g nickelous nitrate (containing NiO25%), 120 DEG C of dryings 4 hours after dipping, 420 DEG C of roastings 3 hours guard catalyst Ib-4 of the present invention.The content adopting X-fluorescence method to measure hydrogenation active metals component in catalyzer lists in table 5.

Embodiment 13

By 100 grams of pseudo-boehmites (Chang Ling catalyst plant produce, butt is 65 % by weight), 3 grams of sesbania powder and 155 grams containing 1.5% nitre aqueous acid.Kneading in double screw banded extruder is also extruded with the cylindrical orifice plate of φ 2.0mm, and dry bar, in 120 DEG C of dryings 4 hours, is pulverized and sieves by wet bar.

Get 40-60 object and sieve to obtain 40 grams, it is mixed with 10 grams of pseudo-boehmites, (Yueyang is polymerized to Chemical Co., Ltd., solid content: 25%) shaping according to roller forming method, and obtaining particle diameter is 5.5-6.5mm spheroidal particle to add 5 grams, water and 15 grams of Alumina gel in the mixture.Afterwards, by this particle in 120 DEG C of dryings 4 hours, 1200 DEG C of roastings 3 hours, obtain carrier Z13.

Adopt X-ray diffraction to characterize, carrier Z13 has Alpha-alumina structure, and adopt pressure mercury method to characterize, carrier Z13 pore distribution curve occurs two peaks at 45-1000 μm and 0.2-1mm, its pore volume, specific surface area and pore distribution value and vehicle group in column in table 4.

Get carrier 20 grams of Z13, in saturated leaching mode with containing 1.45g ammonium molybdate (containing MoO 382%) and the solution 14 milliliters dipping of 1.30g nickelous nitrate (containing NiO 25%), 120 DEG C of dryings 4 hours after dipping, 420 DEG C of roastings 3 hours guard catalyst Ib-5 of the present invention.The content adopting X-fluorescence method to measure hydrogenation active metals component in catalyzer lists in table 5.

Table 4

Table 5

Embodiment 14-19 illustrates that the present invention produces the effect of fine quality catalytic cracking raw material.

Stock oil is: the long residuum that nickel content is 29ppm, content of vanadium is 83ppm, sulphur content is 4.7%, carbon residue is 15% nitrogen content 0.3%.

Evaluating apparatus: 500 milliliters of fixed-bed reactor.

Catalyst combination layering is packed into reactor, and each catalyst levels volume ratio and reaction conditions list in table 6, and operate 300 hours (h) sampling analysis afterwards, the results are shown in table 7.

Hydrodemetalation catalyst Ia:

Hydrodemetalation catalyst Ia-1, prepares according to the embodiment 6 in patent ZL200310117322.6, and it consists of the heavy % of heavy %, the NiO 1.1% of molybdenum oxide 5.5%, balance carriers.

Hydrodemetalation catalyst Ia-2, prepares according to the embodiment 5 in patent ZL200410037670.7, and it consists of the heavy % of heavy %, the NiO 1.5% of molybdenum oxide 7.8%, balance carriers.

Hydrodemetalation catalyst Ia-3, prepares according to the embodiment 13 in patent ZL200410096309.1, and it consists of the heavy % of heavy %, the NiO 1.6% of molybdenum oxide 8.2%, balance carriers.

Hydrotreating catalyst III:

Hydrotreating catalyst III-1, prepares according to the embodiment 6 in patent ZL97112397.7, and it consists of the heavy % of nickel oxide 2.3, the heavy % of Tungsten oxide 99.999 22.0, and the heavy % of fluorine 4, all the other are aluminum oxide.

Hydrotreating catalyst III-2, prepares according to the embodiment 37 in patent ZL00802168.6, and it consists of the heavy % of nickel oxide 2.6, the heavy % of molybdenum oxide 23.6, and the heavy % of fluorine 2.3, all the other are aluminum oxide.

Hydrotreating catalyst III-3, prepares according to the embodiment 3 in patent ZL200310117323.0, and it consists of the heavy % of nickel oxide 2.1, the heavy % of molybdenum oxide 2.5, and the heavy % of Tungsten oxide 99.999 25.4, all the other are aluminum oxide.

In oil sample, the content of nickel and vanadium adopts inductive coupling plasma emission spectrograph (ICP-AES) to measure (instrument is U.S. PE company PE-5300 type plasma quantometer, and concrete grammar is shown in Petrochemical Engineering Analysis method RIPP124-90).In oil sample, sulphur content uses coulometry to measure (concrete grammar is shown in Petrochemical Engineering Analysis method RIPP62-90).In oil sample, carbon residue content uses microdetermination (concrete grammar is shown in Petrochemical Engineering Analysis method RIPP149-90).

Comparative example 5

Catalyzer adopts the combination of Ia-1, D II-1, III-1, and the volume of each catalyst levels when processing condition is listed in table 6, and operate sampling analysis after 300 hours, the results are shown in table 7.

Comparative example 6

Catalyzer adopts the combination of Ia-2, D II-2, III-1, and the volume of each catalyst levels when processing condition is listed in table 6, and operate after 300 hours sampling analysis afterwards, the results are shown in table 7.

Table 6

Table 7

Can find out, adopt raw catalyst and catalyst combination scheme, the foreign matter content such as metal, sulphur, carbon residue of running 300 hours back end hydrogenation treating product obviously reduces, as FCC charging, product property be improved significantly.

Claims (20)

1. the hydrogenation modification method of a catalytically cracked stock, comprise at hydrotreating reaction conditions, described stock oil is contacted with a kind of catalyst combination, described catalyst combination comprises Hydrodemetalation catalyst I, Hydrodemetalation catalyst II and Hydrobon catalyst III, in described catalyst combination the layout of each catalyzer make described stock oil successively with comprise catalyst I, catalyst I I contacts with catalyst I II, by volume and with the total amount of described catalyst combination for benchmark, the content of described catalyst I is 5-60%, the content of catalyst I I is 10-70%, the content of catalyst I II is 5-60%, wherein, described catalyst I I contains carrier, metal component molybdenum, cobalt and nickel, and be selected from the adjuvant component of phosphorus and boron, with oxide basis and with catalyst I I for benchmark, the content of described molybdenum is 5 ~ 20 % by weight, the content sum of cobalt and nickel is 1 ~ 6 % by weight, the content being selected from the adjuvant component of phosphorus and boron is 0.5-5 % by weight, wherein, the atomic ratio of cobalt and nickel is 2 ~ 4.
2. the method according to 1, is characterized in that, in described catalyst I I, the content of molybdenum is 8 ~ 15 % by weight, the content sum of cobalt and nickel is 1.5 ~ 4 % by weight, the content being selected from the adjuvant component of phosphorus and boron is 1 ~ 4 % by weight, and wherein, the atomic ratio of cobalt and nickel is 2.2 ~ 3.2.
3. the method according to 1 or 2, is characterized in that, in described catalyst I I, the content of nickel is less than 1.2%.
4. the method according to 3, is characterized in that, in described catalyst I I, the content of nickel is 0.5 ~ 1.1%.
5. the method according to 1, is characterized in that, by volume and with the total amount of described catalyst combination for benchmark, the content of the content of the catalyst I in described catalyst combination to be the content of 10-50%, catalyst I I be 20-60%, catalyst I II is 10-50%.
6. the method according to 1, it is characterized in that, described catalyst I comprises catalyst I a, described catalyst I a contains carrier, be selected from nickel and/or cobalt, the hydrogenation active metals component of molybdenum and/or tungsten, containing or not containing being selected from boron, phosphorus, one or more adjuvant components in fluorine, with catalyst I a for benchmark, with the content of the nickel of oxide basis and/or cobalt for 0.3-8 % by weight, the content of molybdenum and/or tungsten is 0.5-15 % by weight, boron is selected from element, phosphorus, the content of one or more adjuvant components in fluorine is 0 ~ 5 % by weight, wherein the pore volume of carrier is 0.6-1.4 ml/g, specific surface area is for being greater than 90 to being less than or equal to 350m 2/ g.
7. the method according to 6, is characterized in that, the pore volume of the carrier in described catalyst I a is 0.7-1.2 ml/g, and specific surface area is 100-200m 2/ g.
8. the method according to 6 or 7, is characterized in that, the support selected from alumina in described catalyst I a.
9. the method according to 8, is characterized in that, described aluminum oxide is the alumina supporter with double-hole.
10. the method according to 9, is characterized in that, described double-hole alumina supporter accounts for total pore volume 40-90% at the pore volume of aperture 10-30 nanometer, and aperture accounts for total pore volume 10-60% at the pore volume of 100-2000 nanometer.
11. methods according to 1, it is characterized in that, described catalyst I II contains the carrier being selected from aluminum oxide and/or silica-alumina, be selected from the hydrogenation active metals component of nickel and/or cobalt, molybdenum and/or tungsten, containing or not containing being selected from one or more adjuvant components in fluorine, boron and phosphorus, with catalyst I II for benchmark, be 1 ~ 5 % by weight with the content of the nickel of oxide basis and/or cobalt, the content of molybdenum and/or tungsten is 10 ~ 35 % by weight, is 0 ~ 9 % by weight in the content being selected from one or more adjuvant components in fluorine, boron and phosphorus of element.
12. methods according to 11, is characterized in that, the support selected from alumina in described catalyst I II.
13. methods according to 12, it is characterized in that, the pore volume of described aluminum oxide is not less than 0.35 ml/g, and bore dia is that the pore volume in 40 ~ 100 dust holes accounts for more than 80% of total pore volume.
14. methods according to 6, it is characterized in that, described catalyst I comprises the catalyst I b with catalyst I a layered arrangement, by volume and with described catalyst I a for benchmark, the content of catalyst I b is less than 40%, described layering makes described stock oil contact with catalyst I a with catalyst I b successively, described catalyst I b contains carrier and optionally containing the hydrogenation active metals component being selected from group vib and group VIII, with oxide basis and with catalyst I b for benchmark, the content of the metal component of described group vib is 0 to being less than or equal to 10 % by weight, the content of the metal component of described group VIII is 0 to being less than or equal to 4 % by weight.
15. methods according to 14, it is characterized in that, the carrier of described catalyst I b contains Alpha-alumina, and characterize with mercury penetration method, the pore volume of described carrier is 0.5-0.75ml/g, and specific surface area is 2-20m 2/ g.
16. methods according to 15, it is characterized in that, the pore volume of the carrier of described catalyst I b is 0.52-0.73ml/g, and specific surface area is 5-16m 2/ g, there are two peaks at 45-1000 μm and 0.2-1mm in pore distribution curve.
17. methods according to 16, is characterized in that, the pore distribution curve of the carrier of described catalyst I b occurs two peaks at 45-100 μm and 0.2-1mm.
18. methods according to 14, is characterized in that, by volume and with described catalyst I a for benchmark, the content of catalyst I b is 5-30%.
19. methods according to 1, is characterized in that, the reaction conditions of described hydrotreatment reaction is: hydrogen dividing potential drop 6-20MPa, temperature is 300-450 DEG C, and during liquid, volume space velocity is 0.1-1h -1, hydrogen to oil volume ratio is 600-1500.
20. methods according to 19, is characterized in that, the reaction conditions of described hydrotreatment reaction is: hydrogen dividing potential drop is 10-18MPa, and temperature is 350-420 DEG C, and during liquid, volume space velocity is 0.2-0.6h -1, hydrogen to oil volume ratio is 800-1100.
CN201210107558.0A 2012-04-13 2012-04-13 Hydro-upgrading method of catalytic cracking raw oil CN103374402B (en)

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