CN110038621B - Production method of hydrocracking catalyst - Google Patents

Production method of hydrocracking catalyst Download PDF

Info

Publication number
CN110038621B
CN110038621B CN201810037420.5A CN201810037420A CN110038621B CN 110038621 B CN110038621 B CN 110038621B CN 201810037420 A CN201810037420 A CN 201810037420A CN 110038621 B CN110038621 B CN 110038621B
Authority
CN
China
Prior art keywords
catalyst
aging
mixed solution
acid
weight
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201810037420.5A
Other languages
Chinese (zh)
Other versions
CN110038621A (en
Inventor
王继锋
徐学军
王海涛
刘东香
冯小萍
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Dalian Petrochemical Research Institute Co ltd
China Petroleum and Chemical Corp
Original Assignee
China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Dalian Research Institute of Petroleum and Petrochemicals filed Critical China Petroleum and Chemical Corp
Priority to CN201810037420.5A priority Critical patent/CN110038621B/en
Publication of CN110038621A publication Critical patent/CN110038621A/en
Application granted granted Critical
Publication of CN110038621B publication Critical patent/CN110038621B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J29/166—Y-type faujasite
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/16—Crystalline alumino-silicate carriers
    • C10G47/20—Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects

Landscapes

  • Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a production method of a hydrocracking catalyst. The catalyst is prepared by the steps of carrying out concurrent flow gelling reaction on a mixed solution A containing Ni and W, an organic assistant and a sodium metaaluminate alkaline solution, adding an organic template agent before the gelling reaction, aging the obtained slurry, adding a mixed solution B containing W, Si and Al and ammonia water into the aged slurry in a concurrent flow manner, carrying out the gelling reaction, adding a suspension of a molecular sieve, aging, drying, forming and the like. The hydrocracking catalyst is suitable for medium oil type hydrocracking catalysts, and has good activity and selectivity.

Description

Production method of hydrocracking catalyst
Technical Field
The invention relates to a production method of a hydrocracking catalyst for treating heavy hydrocarbons.
Background
Hydrocracking is carried out under a relatively high pressure, hydrocarbon molecules and hydrogen are subjected to cracking and hydrogenation reactions on the surface of a catalyst to generate a conversion process of lighter molecules, and hydrodesulfurization, denitrification and hydrogenation reactions of unsaturated hydrocarbons also occur. The cracking reaction of the hydrocarbons in the hydrocracking process is carried out on the acidic center of the catalyst, and follows the carbon ion reaction mechanism, and the hydrocarbon isomerization reaction is accompanied with the hydrogenation and cracking reaction.
The hydrocracking catalyst consists of a hydrogenation component and an acid component, the hydrogenation component and the acid component are added according to a certain proportion as required, so that the hydrogenation performance and the cracking performance are balanced, and the hydrocracking catalyst has the function of fully hydrogenating, cracking and isomerizing a hydrocarbon mixture. Therefore, the catalyst required in the distillate oil hydrocracking process should have a strong hydrogenation activity center and a good acid center. The hydrogenation activity is generally provided by metals selected from groups VIB and VIII of the periodic Table of the elements, while the sources of acidity include zeolites and supports such as inorganic oxides.
The cracking activity of the hydrocracking catalyst derives from the acidity of the support component. The acid centers of the hydrocracking catalyst have a strong adsorption effect on nitrogen-containing compounds in the feed, i.e., the nitrogen-containing compounds have poisoning (shielding) effects on the acid centers of the hydrocracking catalyst to different degrees. Therefore, the high-activity hydrocracking catalyst generally has strict limitation on the nitrogen content of the fed material, impurities such as sulfur, nitrogen, oxygen, metals and the like in the raw material are removed through hydrocracking pretreatment, and the nitrogen content of the fed material is generally controlled to be below 10 microgram/g, so that the activity of the hydrocracking catalyst can be fully exerted. Crude oil tends to be heavy and inferior in the world, the sulfur and nitrogen content of the hydrocracking raw oil is high, and meanwhile, the raw material subjected to hydrocracking pretreatment can not meet the requirement of a hydrocracking catalyst on the nitrogen content in the feed at a high airspeed, or the activity stability of the hydrocracking pretreatment catalyst is reduced due to the fact that impurities in the raw material are more, the nitrogen content of the treated raw material can not meet the requirement, and the nitrogen resistance of the hydrocracking catalyst needs to be improved. The hydrocracking catalyst has good nitrogen resistance, can improve the raw material adaptability of the catalyst, and prolongs the operation period of an industrial device.
In general, hydrocracking catalysts may be prepared using methods such as: impregnation, kneading, beating, coprecipitation, etc., and for noble metals, ion exchange, etc. can be used. The impregnation method is to prepare a carrier firstly and then load active metal, the kneading method is to prepare a carrier component firstly and then knead the carrier component and the active metal, and the coprecipitation method is mainly prepared by precipitating an active metal solution, a silicon solution, an aluminum solution and an acid component. Compared with the conventional supported hydrocracking catalyst, the active metal component in the bulk hydrocracking catalyst is not impregnated and supported on a carrier, but oxide of active metal, silicon and aluminum is generated through coprecipitation, and amorphous silica-alumina in the bulk hydrocracking catalyst also provides a certain acidic cracking function and becomes an important component of the acidic component of the bulk hydrocracking catalyst. The metal loading in the bulk hydrocracking catalyst is not limited. The traditional load type hydrocracking catalyst is limited by a carrier pore structure, the load capacity of active metal is generally not more than 30wt%, the number of active centers which can be provided by the load type hydrocracking catalyst is limited, the limit bottleneck of the number of the active centers can not be broken through, the space for greatly improving the hydrogenation activity is limited, and the requirement of a refinery for producing oil products is difficult to meet.
The bulk phase hydrogenation catalyst is usually a VIB group metal element (Mo, W) and a VIII group metal element (Ni), active metal atoms are mutually staggered to provide a reaction space for reactant molecules, and the active metal is exposed on the surface of the catalyst to provide a reaction activity center for the reactant molecules. The supported catalyst is formed by mixing a type of active center with lower activity and a type of active center with higher activity, while the active centers of the bulk catalyst are basically all the type of active centers, and the bulk catalyst greatly improves the catalytic activity of the bulk catalyst mainly by increasing the density of the active centers on the catalyst. Chianelli et al proposed a spoke-edge model to explain the generation of unsupported catalyst active centers, which model models MoS2/WS2The active sites at the edges of the outer layers of the grains are called the spoke sites, provide hydrogenation centers and convert MoS2/WS2The edge active sites of the inner layers of the grains are called edge sites and provide hydrogenolysis centers. Thus, the hydrogenation and hydrogenolysis activities of the catalyst are closely related to the distribution of active sites.
In the reaction process, reactant molecules only react on the surface of the catalyst close to the reactant molecules, active metal on the surface of the catalyst prepared by the existing coprecipitation method is not uniformly dispersed, and meanwhile, the disordered distribution of different hydrogenation active metals causes no good coordination effect among the active metals, so that high-content metal in the bulk phase catalyst is easy to excessively stack metal particles, the generation of an active phase is reduced, the active metal cannot become a hydrogenation active center, the utilization rate of the active metal of the catalyst is influenced, and the use cost of the catalyst is also improved.
A hydrocracking catalyst disclosed in US 3954671, a hydroconversion catalyst disclosed in US 4313817, a hydrocracking catalyst of nitrogen tolerant type productive middle distillate disclosed in CN1253988A, a heavy hydrocarbon hydrocracking catalyst disclosed in CN1253989A, and a high-activity, high-medium oil type hydrocracking catalyst disclosed in CN 101239324A. The catalyst is prepared by coprecipitation method, the acidic mixed solution containing active metal reacts with precipitant to prepare precipitate containing active metal, silicon and aluminum, after adding molecular sieve, the finished product catalyst is prepared by drying, shaping and roasting.
CN201611156531.5 discloses a preparation method of a hydrocracking catalyst. The method comprises the steps of carrying out parallel flow coprecipitation on a mixed aqueous solution of a silicon source, an aluminum source and a nickel salt or a salt of the nickel salt and a metal auxiliary agent M (such as Mo, Co and W) and a precipitator to obtain a precipitation slurry, and aging, forming and roasting to obtain the hydrocracking catalyst.
CN103055923A discloses a preparation method of a hydrocracking catalyst. The method adopts an acidic solution containing hydrogenation active metals, an alkaline solution of sodium metaaluminate and gaseous CO2And adding the mixture into a reaction tank filled with deionized water to form gel, adding suspension of a Y-type molecular sieve, uniformly mixing, filtering, drying, forming, washing, drying and roasting to obtain the hydrocracking catalyst.
CN104588082A discloses a bulk phase hydrocracking catalyst and a preparation method thereof. The method comprises the steps of preparing nickel and aluminum precipitates by a positive addition method, preparing tungsten, silicon and aluminum precipitates by a parallel flow method, mixing the two precipitates, adding Y-type molecular sieve suspension, filtering, forming, roasting and the like to prepare the hydrocracking catalyst.
The above method cannot control the distribution of the hydrogenation active metals well, thereby affecting the distribution of different hydrogenation active metals, being not beneficial to forming effective active phases, being not beneficial to the effective matching of the hydrogenation metals and the acidic components, and finally affecting the performance of the catalyst.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a production method of a hydrocracking catalyst. The method can improve the distribution of hydrogenation active metals in the hydrocracking catalyst, promote the formation and the uniform distribution of an effective active phase of the catalyst, simultaneously uniformly distribute acid components in the catalyst, improve the matching effect between the acid components and the active metal components, and finally improve the activity and the selectivity of the catalyst, and is particularly suitable for the medium oil type hydrocracking catalyst.
The inventor finds that a specific active phase in the hydrocracking catalyst can hydrogenate more organic nitrogen-containing compounds with large toxic action on the acid center of the catalyst more quickly, so that the protection effect on the acid center of the catalyst is achieved, the nitrogen resistance of the hydrocracking catalyst is improved, and the property of a hydrocracking product can be improved.
The invention provides a production method of a hydrocracking catalyst, which comprises the following steps:
(1) preparing a mixed solution A containing Ni and W components, and preparing a mixed solution B containing W, Si and Al components;
(2) adding the mixed solution A, the organic assistant and the sodium metaaluminate alkaline solution into a reaction tank in a concurrent flow manner to carry out gelling reaction to generate precipitate slurry I containing nickel, tungsten and aluminum, and aging the obtained slurry I;
(3) adding the mixed solution B and ammonia water into the aged slurry I obtained in the step (2) in a concurrent flow manner to perform gelling reaction to generate precipitate slurry II containing nickel, tungsten, silicon and aluminum, adding a suspension of a molecular sieve into the slurry II, and then aging under stirring;
(4) after the aging is finished, drying the material obtained in the step (3), forming, washing, drying and roasting to obtain a hydrocracking catalyst;
wherein, an organic template agent is added before the gelling reaction in the step (2).
According to the production method of the hydrocracking catalyst, the hydrocracking catalyst in the step (4) is vulcanized according to the requirement to prepare the vulcanized hydrocracking catalyst.
In the mixed solution A in the step (1), the weight concentration of Ni calculated as NiO is 5-100 g/L, preferably 10-80 g/L, and W calculated as WO3The weight concentration is 2-60 g/L, preferably 10-50 g/L. In the mixed solution B, W is WO3The weight concentration is 2-50 g/L, preferably 4-40 g/L, Si is SiO2The weight concentration is 10-100 g/L, preferably 20-80 g/L, Al is Al2O3The weight concentration is 2-60 g/L, preferably 2-50 g/L. When preparing the mixed solution A, the commonly adopted nickel source can be one or more of nickel sulfate, nickel nitrate and nickel chloride; generally adoptedThe tungsten source is ammonium metatungstate. When preparing the mixed solution B, the tungsten source generally adopted is ammonium metatungstate; the silicon source can be one or more of silica sol, sodium silicate and water glass; the aluminum source can be one or more of aluminum nitrate, aluminum sulfate, aluminum chloride, aluminum acetate and the like.
In the step (2), the organic auxiliary agent is a carboxylic acid polymer and/or an organic phosphonic acid. The molecular weight of the carboxylic acid polymer is 400-5000, the carboxylic acid polymer is selected from one or more of polyacrylic acid, polymethacrylic acid, polymaleic acid, polyaspartic acid, polyepoxysuccinic acid, acrylic acid-hydroxypropyl acrylate copolymer and maleic acid-acrylic acid copolymer, and preferably one or more of polyacrylic acid, polymethacrylic acid, polymaleic acid, polyaspartic acid and polyepoxysuccinic acid. The organic phosphonic acid may be selected from one or more of ethylenediamine tetramethylene phosphonic acid, hydroxyethylene diphosphonic acid, polyol phosphonates, polyaminopolyether methylene phosphonic acid, 1,2, 4-tricarboxylic acid-2-phosphonobutane, hydroxyphosphonoacetic acid, aminotrimethylene phosphonic acid, diethylenetriamine pentamethylene phosphonic acid, preferably from one or more of ethylenediamine tetramethylene phosphonic acid, hydroxyethylene diphosphonic acid, aminotrimethylene phosphonic acid. The molar ratio of the added amount of the organic auxiliary agent to W in the mixed solution A is 0.3: 1-3: 1, preferably 0.5: 1-2: 1.
in the step (2), the organic auxiliary agent may be added separately in parallel, or may be added during the preparation of the mixed solution a, or may be added in combination of the above two ways.
And (3) adding an organic template agent before the gel forming reaction in the step (2), wherein the organic template agent is added into the reaction tank before the reaction, namely before the mixed solution A, the organic auxiliary agent and the sodium metaaluminate alkaline solution are added into the reaction tank in a concurrent flow manner.
The organic template in the step (2) is a quaternary ammonium salt template, preferably one or more of tetraethylammonium bromide, tetraethylammonium hydroxide, tetrapropylammonium bromide, tetrapropylammonium hydroxide, tetrabutylammonium bromide, tetrabutylammonium hydroxide, hexadecyltrimethylammonium bromide and dodecyltrimethylammonium chloride.
The molar ratio of the added amount of the organic template agent to W in the mixed solution A added in the step (2) is 0.3: 1-5: 1, preferably 0.5: 1-4: 1.
w introduced into the catalyst by the mixed solution A in the step (2) accounts for 40-80% of the total W in the catalyst obtained in the step (4) in terms of oxide, and preferably 51-75% in terms of oxide weight. W introduced into the catalyst by the mixed solution B in the step (3) accounts for 20-60%, preferably 25-49% of the total weight of W in the catalyst obtained in the step (4).
Al is introduced into the catalyst in the step (2) through sodium metaaluminate to form Al2O3Accounting for Al in the catalyst obtained in the step (4)2O310wt% to 75wt%, preferably 20wt% to 70wt% of the total weight.
The concentration of the sodium metaaluminate alkaline solution in the step (2) is Al2O3The amount is 15-100 g/L, preferably 20-80 g/L.
In the step (2), the reaction temperature for gelling is 20-90 ℃, preferably 30-70 ℃, the pH value is controlled to be 6.0-10.0, preferably 7.0-9.0, and the gelling time is 0.2-2.0 hours, preferably 0.3-1.5 hours.
The weight concentration of the ammonia water in the step (3) is 5-15%.
And (3) adding the mixed solution B and ammonia water into the aged slurry I in a cocurrent manner to perform gelling reaction under the following reaction conditions: the reaction temperature is 20-90 ℃, preferably 30-80 ℃, the pH value is controlled to be 6.0-11.0, preferably 6.5-9.0, and the gelling time is 0.5-4.0 hours, preferably 1.0-3.0 hours.
The aging conditions in step (2) are as follows: the aging temperature is 40-90 ℃, preferably 50-80 ℃, the pH value during aging is controlled to be 6.0-8.0, preferably 6.5-7.5, and the aging time is 0.1-1.0 hour, preferably 0.2-0.8 hour. The aging is carried out under stirring, the preferred stirring conditions being as follows: the stirring speed is 100-300 rpm, preferably 150-250 rpm.
The aging conditions in step (3) are as follows: the aging temperature is 40-90 ℃, preferably 50-80 ℃, the pH value during aging is controlled to be 7.5-10.0, preferably 7.5-9.0, and the aging time is 1.5-6.0 hours, preferably 2.0-5.0 hours. The aging is carried out under stirring, the preferred stirring conditions being as follows: the stirring speed is 300-500 rpm, preferably 300-450 rpm. The pH of the aging of step (3) is at least 0.5 higher, preferably at least 1.0 higher than the pH of the aging of step (2).
In the step (3), the Si and Al introduced into the catalyst through the mixed solution B account for 20wt% -75 wt%, preferably 25wt% -65 wt%, of the weight of the Si and Al in the catalyst obtained in the step (4), calculated by oxide, wherein the Si accounts for 5wt% -80 wt%, preferably 20wt% -75 wt%, of the total weight of the Si and Al introduced into the catalyst through the mixed solution B, calculated by oxide, calculated by silicon oxide.
The drying, shaping and washing of step (4) may be carried out by methods conventional in the art. Wherein the drying conditions before molding are as follows: drying at 40-180 ℃ for 1-48 hours, preferably at 50-150 ℃ for 4-36 hours. In the forming process, conventional forming aids, such as one or more of peptizers, extrusion aids, and the like, can be added as required. The peptizing agent is one or more of hydrochloric acid, nitric acid, sulfuric acid, acetic acid, oxalic acid and the like, the extrusion aid is a substance beneficial to extrusion forming, such as one or more of sesbania powder, carbon black, graphite powder, citric acid and the like, and the amount of the extrusion aid accounts for 1-10 wt% of the total dry material basis. The washing is generally carried out by washing with deionized water or a solution containing decomposable salts (such as ammonium acetate, ammonium chloride, ammonium nitrate, etc.) until the solution is neutral.
After the molding in the step (4), the drying and baking may be performed by using the conditions conventional in the art, and the drying conditions are as follows: drying for 1-48 hours at 40-180 ℃, wherein the roasting conditions are as follows: roasting at 350-650 ℃ for 1-24 hours, preferably drying under the following conditions: drying for 4-36 hours at 50-150 ℃, and preferably roasting under the following conditions: roasting at 400-600 ℃ for 2-12 hours.
In the method of the invention, the shape of the catalyst can be sheet, spherical, cylindrical strip and special-shaped strip (clover and clover) according to the requirement, the cylindrical strip and the special-shaped strip (clover and clover) are preferred, the diameter of the catalyst can be 0.8-2.0 mm, and the catalyst can also be thick strip with the diameter of more than 2.5 mm.
In the method of the invention, the required catalyst auxiliary agent can be added according to the conventional method, and the auxiliary agent component is Ti and/or Zr. The weight content of the auxiliary component in the hydrocracking catalyst is 20% or less, preferably 15% or less, calculated on an elemental basis. In the preparation of the hydrocracking catalyst of the present invention, it is preferable to add a compound containing an auxiliary component, i.e., a titanium source and/or a zirconium source, during the preparation of the mixed solution a. The titanium source may be one or more of titanium nitrate, titanium sulfate, titanium chloride, etc., and the zirconium source may be one or more of zirconium nitrate, zirconium chloride, zirconium oxychloride, etc.
In the hydrocracking catalyst of the present invention, the molecular sieve used can adopt all the Y-type molecular sieves which can be used in hydrocracking catalysts in the prior art, such as: y-type molecular sieves disclosed in CN102441411A, CN1508228A, CN101450319A and CN 96119840.0. The Y-type molecular sieve disclosed in CN102441411A is preferred in the invention, the molecular sieve reported in CN 96119840.0 is used as a raw material, hydrothermal treatment deep dealumination is carried out under the conditions that the temperature is 650-800 ℃, the pressure is normal pressure to 0.3MPa, and the time is 20-30 hours, a small amount of ammonia can be contained in water vapor during hydrothermal treatment, the ammonia partial pressure is 50-3000 Pa (absolute pressure), then the acid concentration is 0.5-10.0 mol/L, the time is 0.5-20.0 hours, the temperature is 30-80 ℃, and the ratio of the acid dosage to the weight of the molecular sieve is 1: 1-20: 1, using inorganic acid such as hydrochloric acid, sulfuric acid or nitric acid, and obtaining the Y-type molecular sieve suitable for the invention after hydrothermal treatment and acid treatment, wherein the Y-type molecular sieve has the following properties: the specific surface area is 750-900 m2The crystal cell parameter is 2.423 nm-2.545 nm, the relative crystallinity is 95% -110%, and SiO2/Al2O3The molar ratio is 7-60.
The hydrocracking catalyst obtained in the step (4) of the invention is an oxidation state bulk phase hydrocracking catalyst, and can be presulfurized by adopting a conventional method before use. The sulfidation is the conversion of the oxides of the active metals W and Ni into the corresponding sulfides. The vulcanization method can adopt wet vulcanization or dry vulcanization. The vulcanizing method adopted in the invention is wet-process vulcanization, and the vulcanizing agent is a sulfur-containing substance used in conventional vulcanization and can be an organic sulfur-containing substanceOr inorganic sulfur-containing substances, such as one or more of sulfur, carbon disulfide, dimethyl disulfide and the like, wherein the vulcanized oil is hydrocarbons and/or distillate oil, the hydrocarbons are one or more of cyclohexane, cyclopentane, cycloheptane and the like, and the distillate oil is one or more of kerosene, first-line diesel oil, second-line diesel oil and the like. The dosage of the vulcanizing agent is that the vulcanization degree of each active metal in the hydrocracking catalyst is not less than 80%, and can be adjusted according to the actual situation, and the dosage of the vulcanizing agent can be 80-200%, preferably 100-150% of the theoretical sulfur demand of each active metal in the hydrocracking catalyst for complete vulcanization. The prevulcanization conditions are as follows: the temperature is 230-400 ℃, the hydrogen pressure is 5.0-17.0 MPa, and the liquid hourly space velocity is 0.3-4.0 h-1The vulcanization time is 3-24 h, and the preferable selection is as follows: the temperature is 250-370 ℃, the hydrogen pressure is 6.0-16.0 MPa, and the liquid hourly space velocity is 0.5-2.5 h-1And the vulcanization time is 5-16 h.
The sulfuration is to convert the oxide of the active metal component W, Ni into corresponding sulfide to obtain the sulfuration state hydrocracking catalyst, and the sulfuration degree of each active metal in the catalyst is not lower than 80%.
The hydrocracking catalyst prepared by the method is a bulk phase hydrocracking catalyst, and comprises a hydrogenation active metal component and a carrier component, wherein the hydrogenation active metal component is WO3And NiO, after vulcanization, WS2The average number of stacked layers is 5.0 to 7.0 layers, preferably 5.5 to 6.5 layers, WS2The average length of the lamella is 4.0 to 6.0nm, preferably 4.5 to 5.5 nm.
The hydrocracking catalyst prepared by the method has the weight of the hydrocracking catalyst, the content of W in terms of oxide is 10-50 wt%, preferably 15-45 wt%, and the content of Ni in terms of oxide is 3-45 wt%, preferably 5-35 wt%.
In the hydrocracking catalyst prepared by the method, the molar ratio of W to Ni is 0.05-1.2, preferably 0.1-1.0.
The carrier component of the hydrocracking catalyst prepared by the method comprises a molecular sieve and an amorphous oxide, wherein the molecular sieve can be a Y-type molecular sieve; the amorphous oxide is alumina and silica.
The hydrocracking catalyst prepared by the method takes the weight of the hydrocracking catalyst as a reference, and the content of the molecular sieve is 3-30 wt%, preferably 5-25 wt%; the content of the amorphous oxide is 10wt% to 67wt%, preferably 20wt% to 63 wt%.
In the hydrocracking catalyst prepared by the method, the content of the silicon oxide in the amorphous oxide is 3wt% -49 wt%, preferably 5wt% -48 wt% based on the weight of the amorphous oxide.
The hydrocracking catalyst of the invention, after being vulcanized, WS2The number of stacked layers is distributed as follows: the number of the laminated layers with the stacking number of 5.0-7.0 accounts for 55-85% of the total laminated layers, preferably 60-80%; WS2The sheet length distribution is as follows: the number of the lamella with the lamella length of 4.0-6.0 nm accounts for 60.0-85.0% of the total number of the lamellae, and preferably 65.0-80.0%.
The hydrocracking catalyst of the invention, after being vulcanized, WS2The distribution of the number of stacked layers is specifically as follows: the number of the layers with the number of the layers less than 3.0 accounts for 1-8% of the total number of the layers, the number of the layers with the number of the layers from 3.0 to less than 5.0 accounts for 3-15% of the total number of the layers, the number of the layers with the number of the layers from 5.0 to 7.0 accounts for 55-85% of the total number of the layers, and the number of the layers with the number of the layers more than 7.0 accounts for 8-25% of the total number of the layers.
The hydrocracking catalyst of the invention, after being vulcanized, WS2The lamella length distribution is specifically as follows: the number of the lamella with the length of less than 4.0nm accounts for 5.0-25.0% of the total number of the lamellae, the number of the lamella with the length of 4.0-6.0 nm accounts for 60.0-85.0% of the total number of the lamellae, the number of the lamella with the length of more than 6.0-8.0 nm accounts for 1.0-15.0% of the total number of the lamellae, and the number of the lamella with the length of more than 8.0nm accounts for 0.5-4.0% of the total number of the lamellae.
The pore size distribution of the hydrocracking catalyst of the invention is as follows: the pore volume of pores with the diameter of less than 4nm accounts for 5-20% of the total pore volume, the pore volume of pores with the diameter of 4-10 nm accounts for 55-80% of the total pore volume, the pore volume of pores with the diameter of 10-15 nm accounts for 7-20% of the total pore volume, the pore volume of pores with the diameter of more than 15nm accounts for 7-15.0% of the total pore volume, and the preferable pore diameter distribution is as follows: the pore volume of pores with the diameter of less than 4nm accounts for 8-18% of the total pore volume, the pore volume of pores with the diameter of 4-10 nm accounts for 60-75% of the total pore volume, the pore volume of pores with the diameter of 10-15 nm accounts for 8-15% of the total pore volume, and the pore volume of pores with the diameter of more than 15nm accounts for 8-13.0% of the total pore volume.
The hydrocracking catalyst of the invention has the following properties: the specific surface area is 250 to 650m2The pore volume is 0.20 to 0.90 mL/g.
The hydrocracking catalyst of the present invention may contain an auxiliary component as required, the auxiliary component being titanium and/or zirconium, and the weight content of the auxiliary component in the hydrocracking catalyst calculated by element is 20% or less, preferably 15% or less.
The hydrocracking catalyst is particularly suitable for a one-stage series once-through hydrocracking process, and the hydrocracking operation conditions are as follows: the reaction temperature is 300-500 ℃, preferably 350-450 ℃; the pressure is 6-20 MPa, preferably 13-17 MPa; the liquid hourly space velocity is 0.5-3.0 h-1Preferably 0.8 to 2.0 hours-1(ii) a The volume ratio of the hydrogen to the oil is 400-2000: 1, preferably 800-1500: 1.
The hydrocracking catalyst is suitable for heavy raw materials in a wide range, the heavy raw materials comprise one or more of various hydrocarbon oils such as vacuum gas oil, coking gas oil, deasphalted oil, thermal cracking gas oil, catalytic cracking gas oil and catalytic cracking circulating oil, the heavy raw materials usually contain hydrocarbons with the boiling point of 250-550 ℃, the nitrogen content can be 300-2500 mug/g, and after the hydrocracking pretreatment process is carried out, the nitrogen content in the feed of the hydrocracking catalyst is smaller than 150 mug/g, namely the nitrogen content in the feed of a reaction section of the hydrocracking catalyst is smaller than 150 mug/g, further more than 10 mug/g, and even more than 50 mug/g.
The hydrocracking catalyst of the invention, after sulfurization, WS2The stacking layer is high in number and small in length, particularly the stacking layer is concentrated on 5.0-7.0 layers, the length is 4.0-6.0 nm, more effective active phases are generated, the promotion effect between the effective active phases is stronger, and the hydrogenation activity of the catalyst is favorably improved.
The method of the invention firstly uses partial W and Ni in sodium metaaluminate alkaline solution asThe method is carried out under the condition of adding organic auxiliary agent, the active metal and the organic auxiliary agent are chelated to form a macromolecular reticular complex, so that the particles containing W, Ni and Al precipitates after the first primary aging are larger and regularly arranged, the hydrogenation active metal after the post-deposition has a certain anchoring effect, and the active metal after the post-deposition adopts ammonia water as the precipitating agent, so that the post-deposition process is more uniform and mild, different hydrogenation active metals are orderly deposited in the catalyst, the growth speed of metal oxide particles and the probability of mutual contact between the active metals are controlled, and the method is applied to the preparation of the catalyst for the hydrogenation of the hydrogenation active metal3The product has proper particle size and well controlled distribution, and can increase WS in bulk catalyst2The stacking layer number, the lamella length are reduced, the morphology of the active phase is optimized, more effective active phases are generated, and the mutual promotion effect is stronger. Meanwhile, the addition of the organic template agent leads the pore channel of the catalyst to be regular and smooth, the method also leads the catalyst to form a more suitable pore structure, the pore distribution is reasonable, and the specific surface area and the pore volume of the catalyst are improved. In addition, the method of the invention introduces the acid component, can well control the distribution of the acid component, promotes the mutual cooperation between the acid component and the hydrogenation active metal, and is beneficial to improving the activity and the selectivity of the catalyst.
The hydrocracking catalyst still has high activity and stability under the condition of high-nitrogen content feeding (less than 150 mug/g), even can reach the activity equivalent to that of the currently widely applied medium oil type catalyst when the catalyst is operated under low nitrogen (less than 10 mug/g), and meanwhile, the catalyst still has good stability, medium oil selectivity and good product quality when the catalyst is operated under the condition of high nitrogen, and still has good activity stability.
Detailed Description
In the present invention, the specific surface area and the pore volume are measured by a low-temperature liquid nitrogen adsorption method, and the mechanical strength is measured by a side pressure method. In the present invention, WS in bulk catalyst2The number of stacked layers and the length of the sheet layer were measured by a transmission electron microscope. The hydrocracking catalyst of the invention is vulcanized, namely the hydrocracking catalyst is vulcanized into a vulcanized state from a non-vulcanized state hydrocracking catalystThe chemical catalyst is a sulfuration state hydrocracking catalyst. In the present invention, wt% is a mass fraction and v% is a volume fraction.
In the invention, the degree of vulcanization is measured by an X-ray photoelectron spectrometer (XPS), and the percentage of the content of the active metal in a vulcanized state in the total content of the active metal is the degree of vulcanization of the active metal.
Example 1
Respectively dissolving nickel chloride and ammonium metatungstate solution in deionized water, adding 68 g of ethylenediamine tetramethylenephosphonic acid to prepare a mixed solution A, wherein the weight concentration of Ni in the mixed solution A is 42g/L calculated by NiO, and W is WO3The weight concentration was 30 g/L. Respectively dissolving ammonium metatungstate and aluminum chloride solutions in deionized water, adding a dilute water glass solution to prepare a mixed solution B, wherein W in the mixed solution B is WO3The weight concentration is 24g/L, Al is Al2O3The weight concentration is 28g/L, Si is SiO2The weight concentration is 40 g/L. Adding 39 g of tetraethylammonium bromide and deionized water into a reaction tank, and adding Al in a weight concentration2O3And adding 32g/L sodium metaaluminate solution and the mixed solution A into a reaction tank in parallel, keeping the gelling temperature at 65 ℃, controlling the pH value to be 7.5 in the process of parallel-flow gelling reaction, and controlling the gelling time to be 0.6 hour to generate precipitate slurry I containing nickel, tungsten and aluminum. Aging the obtained precipitate slurry I at 75 deg.C for 0.5 hr under the condition of aging pH value of 7.0 and stirring at 200 rpm. After aging, adding the mixed solution B and ammonia water with the weight concentration of 10wt% into the aged slurry I in a cocurrent manner, keeping the gel forming temperature at 58 ℃, controlling the pH value at 7.6 in the cocurrent gel forming reaction process, controlling the gel forming time at 2 hours, obtaining nickel, tungsten, silicon and aluminum precipitate slurry II after the reaction is finished, adding a Y-type molecular sieve suspension (prepared according to CN102441411A example 3) modified by hydrothermal treatment into the precipitate slurry II, adding the Y-type molecular sieve in an amount accounting for 10wt% of the total weight of the catalyst, wherein the property of the Y-type molecular sieve is shown in Table 6, aging under stirring conditions, the stirring rotation speed is 440 r/min, the aging temperature is 75 ℃, the pH value is controlled at 8.6, aging time is 3 hours, filtering the aged slurry, and filtering a filter cake at 100 DEG CDrying for 12 hours, rolling and extruding into strips. Washed 6 times with deionized water at room temperature. The wet strands were then dried at 80 ℃ for 10 hours and calcined at 530 ℃ for 4 hours to give catalyst A. The catalyst composition and the main properties are shown in table 1.
Example 2
According to the method of example 1, according to the component content ratio of the catalyst B in Table 1, adding nickel nitrate, ammonium metatungstate and zirconium oxychloride solution into a dissolving tank 1, adding 178 g of polyacrylic acid (molecular weight is 3000) and 39 g of polymaleic acid (molecular weight is 450) to prepare a mixed solution A, adding ammonium metatungstate and aluminum chloride solution into a dissolving tank 2 to dissolve in deionized water, adding water glass to prepare a mixed solution B, adding 60g of hexadecyl trimethyl ammonium bromide and deionized water into a reaction tank, and adding Al with weight concentration2O3And adding 46g/L sodium metaaluminate solution and the mixed solution A into a reaction tank in parallel, keeping the gelling temperature at 55 ℃, controlling the pH value at 7.1 in the process of parallel-flow gelling reaction, and controlling the gelling time at 0.8 h to generate precipitate slurry I containing nickel, tungsten, aluminum and zirconium. Aging the obtained precipitate slurry I at 77 deg.C for 0.6 hr with the aging pH value controlled at 6.8, and stirring at 210 rpm. After ageing, adding the mixed solution B and 12wt% of ammonia water into the slurry I in a concurrent flow manner, keeping the gelling temperature at 48 ℃, controlling the pH value to be 8.2 in the concurrent flow gelling reaction process, controlling the gelling time to be 2.3 hours, obtaining nickel, tungsten, zirconium, silicon and aluminum precipitate slurry II after the reaction is finished, adding a Y-type molecular sieve suspension (prepared according to CN102441411A example 3) modified by hydrothermal treatment into the precipitate slurry II, adding the Y-type molecular sieve in an amount accounting for 9wt% of the total weight of the catalyst, wherein the property of the Y-type molecular sieve is shown in Table 6, ageing is carried out under stirring conditions, the stirring rotation speed is 405 r/min, the ageing time is 4.1 hours, the ageing temperature is 72 ℃, and the ageing pH value is controlled to be 8.3. Filtering the aged slurry, drying the filter cake at 90 ℃ for 15 hours, extruding into strips for forming, washing with deionized water for 5 times, drying wet strips at 90 ℃ for 10 hours, and roasting at 510 ℃ for 6 hours to obtain the final catalyst B, wherein the composition and main properties of the catalyst are shown in Table 1.
Example 3
According to the method of example 1, according to the component content ratio of catalyst C in Table 1, adding nickel chloride and ammonium metatungstate into dissolving tank 1, adding 38 g hydroxyethylidene diphosphonic acid to prepare mixed solution A, adding aluminum chloride and ammonium metatungstate into dissolving tank 2 to dissolve in deionized water, adding water glass to prepare mixed solution B, adding deionized water and 44 g tetrapropyl ammonium bromide into reaction tank, and adding Al according to the weight concentration2O3Adding 31g/L sodium metaaluminate solution and the mixed solution A into a reaction tank in parallel, keeping the gelling temperature at 55 ℃, controlling the pH value at 8.2 in the process of parallel-flow gelling reaction, and controlling the gelling time at 1.0 hour to generate nickel, tungsten and aluminum containing precipitate slurry I. Aging the obtained precipitate slurry I at 74 ℃ for 0.5 hour under the condition of aging pH value of 6.9 under stirring at 190 rpm. After ageing, adding the mixed solution B and ammonia water with the concentration of 12wt% into the slurry I in a concurrent flow mode, keeping the gelling temperature at 55 ℃, controlling the pH value to be 7.8 in the concurrent flow gelling reaction process, controlling the gelling time to be 2.2 hours, obtaining nickel, tungsten, silicon and aluminum precipitate slurry II after the reaction is finished, adding a Y-type molecular sieve suspension (prepared according to CN102441411A example 3) modified by hydrothermal treatment into the precipitate slurry II, adding the Y-type molecular sieve in an amount accounting for 12wt% of the total weight of the catalyst, wherein the property of the Y-type molecular sieve is shown in Table 6, ageing under the stirring condition, the stirring rotation speed is 390 r/min, the ageing time is 3.9 hours, the ageing temperature is 72 ℃, and the ageing pH value is controlled to be 8.4. Filtering the aged slurry, drying the filter cake at 100 ℃ for 10 hours, extruding into strips, washing with water for 4 times, drying wet strips at 70 ℃ for 16 hours, and roasting at 500 ℃ for 6 hours to obtain the final catalyst C, wherein the composition and the main properties are shown in Table 1.
Example 4
According to the method of example 1, nickel chloride and ammonium metatungstate are added into a dissolving tank 1 according to the component content proportion of a catalyst D in Table 1, 62 g of aminotrimethylene phosphonic acid is added to prepare a mixed solution A, aluminum nitrate and ammonium metatungstate are added into a dissolving tank 2 to be dissolved in deionized water, and water glass is added to prepare a mixed solution B. 23 grams of tetraethylammonium hydroxide and deionized water were added to the reaction tank and the weight was concentratedDegree is based on Al2O3Adding 48g/L sodium metaaluminate solution and the mixed solution A into a reaction tank in parallel, keeping the gelling temperature at 50 ℃, controlling the pH value at 7.3 in the process of parallel-flow gelling reaction, and controlling the gelling time at 1.2 hours to generate precipitate slurry I containing nickel, tungsten and aluminum. Aging the obtained precipitate slurry I at 78 deg.C for 0.7 hr at an aging pH of 7.0 under stirring at 220 rpm. After ageing, adding the mixed solution B and 8wt% ammonia water into the slurry I in a concurrent flow manner, keeping the gelling temperature at 50 ℃, controlling the pH value at 8.3 in the concurrent flow gelling reaction process, controlling the gelling time at 2.4 hours, obtaining nickel, tungsten, silicon and aluminum precipitate slurry II after the reaction is finished, adding a Y-type molecular sieve suspension (prepared according to CN102441411A example 3) modified by hydrothermal treatment into the precipitate slurry II, adding the Y-type molecular sieve in an amount accounting for 9wt% of the total weight of the catalyst, wherein the property of the Y-type molecular sieve is shown in Table 6, ageing under stirring conditions, the stirring rotation speed is 400 r/min, the ageing time is 4.3 hours, the ageing temperature is 74 ℃, and the ageing pH value is controlled at 8.4. Filtering the aged slurry, drying the filter cake at 90 ℃ for 12 hours, extruding into strips for forming, washing with deionized water for 3 times, drying wet strips at 100 ℃ for 8 hours, and roasting at 480 ℃ for 5 hours to obtain the final catalyst D, wherein the composition and the main properties are shown in Table 1.
Comparative example 1
The catalyst prepared according to the method disclosed in CN101239324A has the same composition as that of example 1, and comprises the following specific steps:
(1) respectively mixing nickel chloride, aluminum chloride and ammonium metatungstate solution deionized water in a 5L reaction tank, and adding 1000 ml of deionized water for dilution;
(2) preparation of a mixture containing SiO as in example 12Adding the (2) into the (1) with stirring the dilute water glass solution with the same content;
(3) adding ammonia water into the mixture of (1) and (2) under stirring until the pH value is 5.2;
(4) the configuration contains WO in example 13Adding sodium tungstate solution with the same content into the mixture of (1) + (2) + (3) under stirring;
(5) continuously adding ammonia water until the pH value is 7.6;
(6) the whole gelling process is carried out at 60 ℃;
(7) standing and aging the mixture at 75 ℃ for 3.5 hours, and controlling the pH value to be 7.8 after the aging is finished; a suspension of Y-type molecular sieve (prepared according to CN102441411A example 3) added before aging, wherein the Y-type molecular sieve is added in an amount of 10wt% based on the total weight of the catalyst, and the properties of the Y-type molecular sieve are shown in Table 6;
(8) filtering, drying in an oven at 100 deg.C for 12 hr, grinding, and extruding with a 3 mm-diameter orifice plate; washing with ammonium acetate solution pH =8.8 at room temperature; then dried in an oven at 80 ℃ for 10 hours and roasted at 530 ℃ for 4 hours to obtain a reference agent E, and the composition and the main properties of the catalyst are shown in Table 1.
Comparative example 2
The catalyst is prepared according to the method disclosed in CN103055923A, has the same composition as the catalyst in the example 1, and comprises the following specific steps:
(1) preparing an acid solution A: nickel chloride and ammonium metatungstate were mixed in a 5l vessel and diluted with 1000 ml of deionized water according to the catalyst composition of example 1. Preparation of a mixture containing SiO as in example 12The same amount of dilute water glass solution was added to the above mixed salt solution with stirring.
(2) Preparing an alkaline solution B: the formulation contains Al as in example 12O3Alkaline sodium metaaluminate solution with the same content.
(3) Mixing solution A, solution B and CO2And adding the gas into a gelatinizing tank in a parallel flow manner to gelatinize, wherein the gelatinizing temperature is kept at 60 ℃, and the pH value is 7.6. Wherein CO is used2Gas concentration 45v%, CO addition2Total amount of gas and Al in alkaline solution2O3The molar ratio is 3, and the flow rate of A, B solution is adjusted to ensure that the simultaneous dripping is finished so as to ensure that the catalyst is uniformly distributed and the composition is not changed.
(4) After the completion of the gelling, a suspension of Y-type molecular sieve (prepared according to CN102441411A example 3) was added under stirring, the amount of Y-type molecular sieve was 10wt% based on the total weight of the catalyst, the properties of the Y-type molecular sieve are shown in table 6, and the Y-type molecular sieve was uniformly dispersed in the mixed slurry obtained by gelling, and left to stand at about 75 ℃ for aging for 3.5 hours.
(5) And (4) filtering the material obtained in the step (4), drying a filter cake for 12 hours at 100 ℃, rolling, extruding and forming. Washed with deionized water at room temperature. Then dried at 80 ℃ for 10 hours and calcined at 530 ℃ for 4 hours to obtain a catalyst F. The catalyst composition and the main properties are shown in table 1.
Comparative example 3
In the preparation process of comparative example 3, the active metal, silicon and aluminum solution and the precipitant are reacted at one time to generate nickel, tungsten, silicon and aluminum precipitate slurry, and the stepwise reaction and the secondary aging are not performed. The catalyst composition is the same as that of example 1, and the specific steps are as follows:
respectively dissolving nickel chloride, aluminum chloride, ammonium metatungstate and water glass in deionized water to prepare a mixed solution, wherein the weight concentration of NiO in the mixed solution is 42g/L, and Al2O3Has a weight concentration of 45g/L, WO3Has a weight concentration of 31g/L, SiO2The weight concentration of (B) is 40 g/L. Adding 500mL of deionized water into a reaction tank, adding 10wt% ammonia water and the mixed solution into the reaction tank in a concurrent flow manner, keeping the gelling temperature at 60 ℃, controlling the pH value at 7.6 in the concurrent flow gelling reaction process, and controlling the gelling time at 2.5 hours to generate precipitate slurry containing nickel, tungsten, silicon and aluminum. Adding a Y-type molecular sieve suspension modified by hydrothermal treatment (prepared according to CN102441411A example 3) into the precipitate slurry, wherein the addition amount of the Y-type molecular sieve is 10wt% of the total weight of the catalyst, the properties of the Y-type molecular sieve are shown in Table 6, uniformly stirring, aging, controlling the aging temperature at 75 ℃, the pH value at 7.8 and the aging time at 3.5 hours, filtering the aged slurry, drying a filter cake at 120 ℃ for 8 hours, rolling, extruding and forming. Washed 6 times with deionized water at room temperature. The wet strands were then dried at 80 ℃ for 10 hours and calcined at 530 ℃ for 4 hours to give catalyst G. The catalyst composition and the main properties are shown in table 1.
Comparative example 4
The catalyst is prepared according to the method disclosed in CN104588082A, has the same composition as the catalyst in the example 1, and comprises the following specific steps:
adding nickel nitrate and aluminum chloride solution into the dissolving tank 1 to prepare working solution A, and adding aluminum chloride, ammonium metatungstate and dilute water glass into the dissolving tank 2 to prepare working solution B. Adding ammonia water into the solution A under stirring, keeping the gelling temperature at 60 ℃, controlling the pH value at 7.6 when the gelling is finished, and controlling the gelling time at 30 minutes to generate nickel and aluminum containing precipitate slurry I. Adding 500mL of deionized water into a reaction tank, adding ammonia water and the solution B into the reaction tank in a cocurrent manner, keeping the gelling temperature at 60 ℃, controlling the pH value to be 7.8 in the cocurrent gelling reaction process, and controlling the gelling time to be 2 hours to generate precipitate slurry II containing tungsten, silicon and aluminum. Mixing the two types of slurry containing the precipitate, adding a Y-shaped molecular sieve suspension (prepared according to CN102441411A example 3) modified by hydrothermal treatment into the two types of slurry containing the precipitate under the condition of continuous stirring, wherein the addition amount of the Y-shaped molecular sieve accounts for 10wt% of the total weight of the catalyst, the property of the Y-shaped molecular sieve is shown in Table 6, uniformly dispersing the Y-shaped molecular sieve in the mixed slurry obtained by gelling, aging at 75 ℃ for 3.5 hours, filtering, drying at 100 ℃ for 12 hours, rolling, extruding and forming. Washed with ionized water at room temperature. Then dried at 80 ℃ for 10 hours and calcined at 530 ℃ for 4 hours to obtain a catalyst H. The catalyst composition and the main properties are shown in table 1.
Example 5
This example is WS in the sulfided catalyst2Average wafer length and average number of stacked layers. The TEM picture of the prepared bulk phase catalyst is subjected to statistical analysis, and the statistical area is about 20000nm2Statistical WS2The total number of slices exceeds 400. Bulk phase catalyst WS according to the calculation formulae (1) and (2)2The average length of the sheets and the average number of stacked layers were statistically calculated and the results are shown in Table 3.
Figure DEST_PATH_IMAGE002
（1）
Figure DEST_PATH_IMAGE004
（2）
In the formulas (1) and (2),L A is WS2The average length of the sheets is,L i is WS2Lamella length, nm;n i is of length ofL i WS (A) of2The number of the sheets is equal to the number of the sheets,N A is WS2The average number of stacked layers;N i is WS2The number of layers is stacked,m i is stacked with the number of layers ofN i WS (A) of2Number of slices.
The catalyst A, B, C, D of the invention and the catalyst E, F, G, H of the comparative example were used to perform sulfidation on a hydrogenation microreactor, the catalyst loading volume was 10mL, and the sulfiding agent was CS2The sulfurized oil being cyclohexane, CS2The amount of sulfur used is 110% of the theoretical amount of sulfur required. The prevulcanization conditions are as follows: the temperature is 350 ℃, the hydrogen pressure is 14.5MPa, and the liquid hourly volume space velocity is 2.0h-1And the time is 10 h.
Example 6
This example is an evaluation experiment of the activity of the catalyst of the present invention and is compared with the catalyst of the comparative example. A comparative evaluation test was conducted on a 200mL compact hydrogenation apparatus using the A, B, C, D catalyst of the present invention and the E, F, G, H catalyst of comparative example under the following conditions: the total reaction pressure is 14.7MPa, the volume ratio of hydrogen to oil is 1200, and the liquid hourly space velocity is 1.5h-1The evaluation raw material was Sauter VGO heavy distillate oil, and the main properties thereof are shown in Table 4, and Table 5 shows the evaluation results of the catalyst after 500 hours of operation.
As can be seen from Table 2, the catalysts of the present invention have WS as compared with the catalysts of the comparative examples without substantially changing the amount of active metal2The stacking layer number is increased, the average length of the lamella is reduced, and the number of hydrogenation active centers is obviously increased. From the results of the evaluation, table 5 shows that the activity and the middle oil selectivity of the catalyst A, B, C, D prepared by the present invention are superior to those of the reference. The catalyst prepared by the method has high utilization rate of active metal, and the hydrogenation reaction activity of the catalyst is obviously improved.
By adopting the catalyst A of the invention, the catalyst is continuously operated for 2500 hours under the operating conditions, and the product yield and the property are basically not changed, which shows that the hydrocracking catalyst of the invention has good activity and stability for processing high-nitrogen raw materials. While the catalyst E, F, G, H of the comparative example is required to continuously increase the reaction temperature under the condition of ensuring the initial product yield and properties, the product yield and properties are obviously reduced even after the reaction temperature is increased for 2500 hours of continuous operation due to serious catalyst deactivation.
TABLE 1 compositions and Properties of catalysts prepared in examples and comparative examples
Catalyst numbering A B C D E F G H
Catalyst composition
NiO，wt% 19 16 18 22 19 19 19 19
WO3，wt% 28 34 32 31 28 28 28 28
SiO2，wt% 22 21 21 22 22 22 22 22
Al2O3，wt% 31 26 29 25 31 31 31 31
Others, wt.% - ZrO2/3.0 - - - - - -
Catalyst Properties
Specific surface area, m2/g 401 396 394 395 354 391 365 375
Pore volume, mL/g 0.423 0.416 0.418 0.417 0.365 0.415 0.381 0.389
Mechanical Strength, N/mm 19.4 19.6 20.1 20.1 17.7 17.8 17.1 17.3
Hole distribution,%
＜4nm 7.23 7.66 7.81 7.73 56.12 13.46 45.35 44.02
4nm~10nm 69.90 69.34 69.53 69.40 30.12 46.08 38.05 38.39
10nm~15nm 12.35 12.41 12.18 12.09 8.11 36.06 8.38 9.13
＞15nm 10.52 10.59 10.48 10.78 5.65 4.40 8.22 8.46
TABLE 2 WS in catalysts obtained in examples and comparative examples2Average number of stacked layers and average sheet length of
Catalyst numbering Average number of stacked layers NA Average lamella length LA，nm
A 6.42 4.78
B 6.34 4.81
C 6.32 4.84
D 6.33 4.85
E 4.02 6.68
F 4.18 6.89
G 3.98 7.01
H 4.05 6.92
TABLE 3 WS in bulk catalysts2Distribution of the number of stacked layers and the length of the sheet
Catalyst numbering A B C D E F G H
Distribution of number of lamellae,%
< 3 layers 2.54 2.87 2.95 2.83 15.35 13.25 14.93 14.85
3 to less than 5 layers 9.49 9.71 9.91 10.19 76.25 75.95 75.09 75.26
5 to 7 layers 76.68 76.42 76.23 76.11 7.38 9.05 8.11 7.91
Greater than 7 layers 11.29 11.00 10.91 10.87 1.02 1.75 1.87 1.98
Length distribution of%
＜4nm 17.89 17.84 17.77 17.66 5.69 5.26 6. 08 4.99
4~6nm 76.16 75.94 76.07 76.01 12.36 13.95 14.02 14.21
Greater than 6 to 8nm 5.08 5.15 5.26 5.30 71.25 72.22 71.94 72.08
＞8nm 0.87 1.07 0.90 1.03 10.70 8.57 7.96 8.72
TABLE 4 Primary Properties of the base oils
Item Analysis results
Density (20 ℃ C.), g/cm3 0.9205
Range of distillation range, deg.C 314-539
S，µg/g 10100
N，µg/g 1920
Carbon residue in wt% 0.18
Freezing point, deg.C 33
TABLE 5 catalyst evaluation results
Catalyst numbering A B C D
Reaction temperature of 389 390 389 390
Nitrogen content in the feed, microgram/g 108.0 92.9 82.5 96.4
Product distribution and Properties, wt.%
Heavy naphtha (82-138 ℃ C.)
Yield, wt.% 7.6 8.0 8.0 7.8
Aromatic hydrocarbon, wt% 52.5 52.4 52.1 52.2
Jet fuel (138-249 deg.C)
Yield, wt.% 28.3 28.2 28.3 28.4
Smoke point, mm 32 33 31 32
Diesel oil (249-371 deg.C)
Yield, wt.% 28.6 28.5 28.4 28.3
Cetane number 71.0 70.8 70.7 70.8
Tail oil (A)>371℃）
Yield, wt.% 30.5 30.6 30.6 30.5
BMCI value 5.9 6.3 6.1 6.4
Medium oil selectivity, wt% 81.9 81.7 81.7 81.6
TABLE 5 continuation
Catalyst numbering E F G H
Reaction temperature of 396 396 395 396
Nitrogen content in the feed, microgram/g 90.6 105.9 102.7 89.4
Product distribution, wt%
Heavy naphtha (82-138 ℃ C.)
Yield, wt.% 9.8 10.0 9.9 9.7
Aromatic hydrocarbon, wt% 63.6 62.1 63.3 62.8
Jet fuel (138-249 deg.C)
Yield, wt.% 18.2 18.8 19.0 18.9
Smoke point, mm 22 24 24 23
Diesel oil (249-371 deg.C)
Yield, wt.% 20.4 20.2 19.9 20.1
Cetane number 61.5 61.9 60.8 61.1
Tail oil (A)>371℃）
Yield, wt.% 42.0 42.2 42.1 42.5
BMCI value 18.5 20.9 19.1 21.6
Medium oil selectivity, wt% 66.5 67.5 67.1 67.8
TABLE 6 Properties of modified Y-type molecular sieves relating to examples and comparative examples
Relative degree of crystallinity,% 95
Cell parameter, nm 2.439
SiO2/Al2O3，mol/mol 12.05
Specific surface area, m2/g 839
Pore volume, mL/g 0.506
1.7 to 10nm secondary pores occupying the total pore volume% 48.0
Total infrared acid, mmol/g 0.999
Na2O，wt% 0.093

Claims (44)

1. A method for producing a hydrocracking catalyst, comprising:
(1) preparing a mixed solution A containing Ni and W components, and preparing a mixed solution B containing W, Si and Al components;
(2) adding the mixed solution A, the organic assistant and the sodium metaaluminate alkaline solution into a reaction tank in a concurrent flow manner to carry out gelling reaction to generate precipitate slurry I containing nickel, tungsten and aluminum, and aging the obtained slurry I;
(3) adding the mixed solution B and ammonia water into the aged slurry I obtained in the step (2) in a concurrent flow manner to perform gelling reaction to generate precipitate slurry II containing nickel, tungsten, silicon and aluminum, adding a suspension of a molecular sieve into the slurry II, and then aging under stirring;
(4) after the aging is finished, drying the material obtained in the step (3), forming, washing, drying and roasting to obtain a hydrocracking catalyst;
wherein, an organic template agent is added before the gelling reaction in the step (2); the organic template is a quaternary ammonium salt template; in the step (2), the organic auxiliary agent is a carboxylic acid polymer and/or an organic phosphonic acid; the molecular weight of the carboxylic acid polymer is 400-5000.
2. The method of claim 1, wherein: in the mixed solution A in the step (1), the weight concentration of Ni in NiO is 5-100 g/L, and W in WO3The calculated weight concentration is 2-60 g/L; in the mixed solution B, W is WO3The weight concentration is 2-50 g/L, Si is SiO2The weight concentration is 10-100 g/L, Al is Al2O3The weight concentration is 2-60 g/L.
3. The method of claim 1, wherein: the carboxylic acid polymer is one or more of polyacrylic acid, polymethacrylic acid, polymaleic acid, polyaspartic acid, polyepoxysuccinic acid, acrylic acid-hydroxypropyl acrylate copolymer and maleic acid-acrylic acid copolymer; the organic phosphonic acid is one or more of ethylenediamine tetramethylene phosphonic acid, hydroxyethylidene diphosphonic acid, polyalcohol phosphonate ester, polyamino polyether methylene phosphonic acid, 1,2, 4-tricarboxylic acid-2-phosphonic butane, hydroxyphosphonoacetic acid, aminotrimethylene phosphonic acid and diethylenetriamine pentamethylene phosphonic acid; the molar ratio of the added amount of the organic auxiliary agent to W in the mixed solution A is 0.3: 1-3: 1.
4. a method according to claim 3, characterized by: the carboxylic acid polymer is one or more of polyacrylic acid, polymethacrylic acid, polymaleic acid, polyaspartic acid and polyepoxysuccinic acid; the organic phosphonic acid is one or more of ethylenediamine tetramethylene phosphonic acid, hydroxyethylidene diphosphonic acid and amino trimethylene phosphonic acid; the molar ratio of the added amount of the organic auxiliary agent to W in the mixed solution A is 0.5: 1-2: 1.
5. the method of claim 1, wherein: in the step (2), the organic auxiliary agent is added separately in parallel flow, or is added when the mixed solution A is prepared, or is added by combining the two modes.
6. The method of claim 1, wherein: the organic template agent in the step (2) is one or more of tetraethylammonium bromide, tetraethylammonium hydroxide, tetrapropylammonium bromide, tetrapropylammonium hydroxide, tetrabutylammonium bromide, tetrabutylammonium hydroxide, hexadecyltrimethylammonium bromide and dodecyltrimethylammonium chloride.
7. The method of claim 1, wherein: the molar ratio of the added amount of the organic template agent in the step (2) to W in the mixed solution A added in the step (2) is 0.3: 1-3: 1.
8. the method of claim 1, wherein: the molar ratio of the added amount of the organic template agent in the step (2) to W in the mixed solution A added in the step (2) is 0.5: 1-2: 1.
9. the method of claim 1, wherein: and (3) adding an organic template agent before the gel forming reaction in the step (2), namely adding the organic template agent into the reaction tank before the mixed solution A, the organic auxiliary agent and the sodium metaaluminate alkaline solution are added into the reaction tank in a parallel flow manner.
10. The method of claim 1, wherein: w introduced into the catalyst from the mixed solution A by the step (2) and WO3In the catalyst WO340 to 80 percent of the total weight of the composition; w introduced into the catalyst from the mixed solution B by the step (3) and WO3In the catalyst WO320 to 60 percent of the total weight of the composition.
11. The method of claim 1, wherein: w introduced into the catalyst from the mixed solution A by the step (2) and WO3In the catalyst WO351 to 75 percent of the total weight of the composition; w introduced into the catalyst from the mixed solution B by the step (3) and WO3In the catalyst WO325 to 49% by weight of (A).
12. The method of claim 1, wherein: al is introduced into the catalyst in the step (2) through sodium metaaluminate to form Al2O3Accounting for Al in the catalyst obtained in the step (4)2O310wt% -75 wt% of the weight.
13. The method of claim 1, wherein: al is introduced into the catalyst in the step (2) through sodium metaaluminate to form Al2O3Accounting for Al in the catalyst obtained in the step (4)2O320wt% -70 wt% of the weight.
14. The method of claim 1, wherein: in the step (3), the Si and Al introduced into the catalyst through the mixed solution B account for 20-75 wt% of the weight of the Si and Al in the catalyst obtained in the step (4) in terms of oxide, wherein the Si accounts for 5-80 wt% of the total weight of the Si and Al introduced into the catalyst through the mixed solution B in terms of silicon oxide.
15. The method of claim 1, wherein: in the step (3), the Si and Al introduced into the catalyst through the mixed solution B account for 25-65 wt% of the weight of the Si and Al in the catalyst obtained in the step (4) in terms of oxide, wherein the Si accounts for 20-75 wt% of the total weight of the Si and Al introduced into the catalyst through the mixed solution B in terms of silicon oxide.
16. The method of claim 1, wherein: in the step (2), the concentration of the sodium metaaluminate alkaline solution is Al2O3The amount is 15-100 g/L.
17. The method of claim 1, wherein: in the step (2), the concentration of the sodium metaaluminate alkaline solution is Al2O3The amount is 20-80 g/L.
18. The method of claim 1, wherein: the gelling reaction conditions in the step (2) are as follows: the reaction temperature is 20-90 ℃, the pH value is controlled to be 6.0-10.0, and the gelling time is 0.2-2.0 hours.
19. The method of claim 1, wherein: the gelling reaction conditions in the step (2) are as follows: the reaction temperature is 30-70 ℃, the pH value is controlled to be 7.0-9.0, and the gelling time is 0.3-1.5 hours.
20. The method of claim 1, wherein: the weight concentration of the ammonia water in the step (3) is 5-15%.
21. The method of claim 1, wherein: in the step (3), the gelling reaction conditions are as follows: the reaction temperature is 20-90 ℃, the pH value is controlled to be 6.0-11.0, and the gelling time is 0.5-4.0 hours.
22. The method of claim 1, wherein: in the step (3), the gelling reaction conditions are as follows: the reaction temperature is 30-80 ℃, the pH value is controlled to be 6.5-9.0, and the gelling time is 1.0-3.0 hours.
23. The method of claim 1, wherein: the aging conditions in step (2) are as follows: the aging temperature is 40-90 ℃, the pH value during aging is controlled to be 6.0-8.0, and the aging time is 0.1-1.0 hour; aging was carried out under stirring.
24. The method of claim 1, wherein: the aging conditions in step (2) are as follows: the aging temperature is 50-80 ℃, the pH value during aging is controlled to be 6.5-7.5, and the aging time is 0.2-0.8 hours; aging was carried out under stirring under the following conditions: the stirring speed is 100-300 rpm.
25. The method of claim 1, wherein: the aging conditions in step (3) are as follows: the aging temperature is 40-90 ℃, the pH value during aging is controlled to be 7.5-10.0, and the aging time is 1.5-6.0 hours; aging was carried out under stirring.
26. The method of claim 1, wherein: the aging conditions in step (3) are as follows: the aging temperature is 50-80 ℃, the pH value during aging is controlled to be 7.5-9.0, and the aging time is 2.0-5.0 hours; aging was carried out under stirring under the following conditions: the stirring speed is 300-500 rpm.
27. A method according to claim 1 or 25, characterized by: the aged pH of step (3) is at least 0.5 higher than the aged pH of step (2).
28. A method according to claim 1 or 25, characterized by: the aged pH of step (3) is at least 1.0 higher than the aged pH of step (2).
29. The method of claim 1, wherein: the molecular sieve in the step (3) is a Y-type molecular sieve, and has the following properties: the specific surface area is 750-900 m2The crystal cell parameter is 2.423 nm-2.545 nm, the relative crystallinity is 95% -110%, and SiO2/Al2O3The molar ratio is 7-60.
30. The method of claim 1, wherein: the drying conditions in step (4) before molding are as follows: drying for 1-48 hours at 40-180 ℃; after the step (4) of molding, the adopted drying conditions are as follows: drying for 1-48 hours at 40-180 ℃, wherein the roasting conditions are as follows: roasting at 350-650 ℃ for 1-24 hours.
31. The method of claim 1, wherein: the hydrocracking catalyst contains auxiliary agents Ti and/or Zr; the weight content of the auxiliary component in the hydrocracking catalyst is less than 20 percent in terms of element; in the preparation process of the hydrocracking catalyst, a compound containing an auxiliary component is added in the preparation process of the mixed solution A.
32. The method of claim 1, wherein: and (4) sulfurizing the hydrocracking catalyst in the step (4) to prepare a sulfurized hydrocracking catalyst, wherein the sulfurization degree of each active metal in the catalyst is not lower than 80%.
33. The method of claim 32, wherein: the sulfurization is to convert the active metal W, Ni into corresponding sulfide, the sulfurization method adopts wet sulfurization, the sulfurization agent is organic sulfur-containing substance and/or inorganic sulfur-containing substance, one or more selected from sulfur, carbon disulfide, dimethyl disulfide, the sulfurized oil is hydrocarbon and/or distillate oil, wherein the hydrocarbon is one or more selected from cyclohexane, cyclopentane, cycloheptane, the distillate oil is one or more selected from kerosene, normal first-line diesel oil, normal second-line diesel oil; the prevulcanization conditions are as follows: the temperature is 230-400 ℃, the hydrogen pressure is 5.0-17.0 MPa, and the liquid hourly space velocity is 0.3-4.0 h-1And the vulcanization time is 3-24 h.
34. The method of claim 33, wherein: the prevulcanization conditions are as follows: the temperature is 250-370 ℃, the hydrogen pressure is 6.0-16.0 MPa, and the liquid hourly space velocity is 0.5-2.5 h-1And the vulcanization time is 5-16 h.
35. The method of claim 1, wherein: the hydrocracking catalyst obtained in the step (4) takes the weight of the hydrocracking catalyst as a reference, the content of W in terms of oxide is 10-50 wt%, and the content of Ni in terms of oxide is 3-45 wt%.
36. The method of claim 1, wherein: the hydrocracking catalyst obtained in the step (4) takes the weight of the hydrocracking catalyst as a reference, the content of W in terms of oxide is 15wt% -45 wt%, and the content of Ni in terms of oxide is 5wt% -35 wt%.
37. A method according to claim 35 or 36, wherein: the molar ratio of W to Ni is 0.05 to 1.2.
38. A method according to claim 35 or 36, wherein: the molar ratio of W to Ni is 0.1 to 1.0.
39. The method of claim 1, wherein: the content of the molecular sieve is 3-30 wt% based on the weight of the hydrocracking catalyst; the content of the amorphous oxide is 10-67 wt%; the amorphous oxide is alumina and silica, and the content of the silica in the amorphous oxide is 3-19 wt% based on the weight of the amorphous oxide.
40. The method of claim 1, wherein: the content of the molecular sieve is 5-25 wt% based on the weight of the hydrocracking catalyst; the content of the amorphous oxide is 20-63 wt%; the amorphous oxide is alumina and silicon oxide, and the content of the silicon oxide in the amorphous oxide is 5-48 wt% based on the weight of the amorphous oxide.
41. A method according to claim 1 or 32, characterized by: after said hydrocracking catalyst has been sulphided, WS2An average number of stacked layers of 5.0 to 7.0, WS2The average length of the lamella is 4.0-6.0 nm.
42. A method according to claim 1 or 32, characterized by: after said hydrocracking catalyst has been sulphided, WS2An average number of stacked layers of 5.5 to 6.5, WS2The average length of the lamella is 4.5-5.5 nm.
43. A method according to claim 1 or 32, characterized by: after said hydrocracking catalyst has been sulphided, WS2The number of stacked layers is distributed as follows: the number of the stacked layers is 5.0-7.0, and the number of the layers accounts for 55-85% of the total number of the layers; WS2The sheet length distribution is as follows: the number of the lamella with the lamella length of 4.0-6.0 nm accounts for 60.0-85.0% of the total number of the lamellae.
44. A method according to claim 1 or 32, characterized by: after said hydrocracking catalyst has been sulphided, WS2The number of stacked layers is distributed as follows: the number of stacked layers is 5.0-7.0, and the number of the stacked layers accounts for 60-80% of the total number of the stacked layers; WS2The sheet length distribution is as follows: the number of the sheets with the length of 4.0-6.0 nm accounts for 65.0-80.0% of the total number of the sheets.
CN201810037420.5A 2018-01-16 2018-01-16 Production method of hydrocracking catalyst Active CN110038621B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201810037420.5A CN110038621B (en) 2018-01-16 2018-01-16 Production method of hydrocracking catalyst

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810037420.5A CN110038621B (en) 2018-01-16 2018-01-16 Production method of hydrocracking catalyst

Publications (2)

Publication Number Publication Date
CN110038621A CN110038621A (en) 2019-07-23
CN110038621B true CN110038621B (en) 2021-12-07

Family

ID=67272823

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810037420.5A Active CN110038621B (en) 2018-01-16 2018-01-16 Production method of hydrocracking catalyst

Country Status (1)

Country Link
CN (1) CN110038621B (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112791741B (en) * 2019-11-14 2023-07-25 中国石油天然气股份有限公司 Preparation method of hydrocracking catalyst
CN114014337B (en) * 2022-01-05 2022-03-15 中汽研（天津）汽车工程研究院有限公司 AEI-CHA intergrowth molecular sieve and catalyst thereof

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103769125A (en) * 2012-10-24 2014-05-07 中国石油化工股份有限公司 Preparation method of hydro-treatment catalyst
CN104588076A (en) * 2013-11-03 2015-05-06 中国石油化工股份有限公司 Hydrocracking catalyst and preparation method thereof
CN104588082A (en) * 2013-11-03 2015-05-06 中国石油化工股份有限公司 Hydrocracking catalyst preparation method
CN104588086A (en) * 2013-11-03 2015-05-06 中国石油化工股份有限公司 Preparation method of hydrocracking catalyst

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ATE296163T1 (en) * 1999-04-08 2005-06-15 Albemarle Netherlands Bv METHOD FOR SULFIDATION OF AN ORGANIC NITROGEN AND CARBONYL HYDROTREATMENT CATALYST
FR2875419B1 (en) * 2004-09-22 2007-02-23 Inst Francais Du Petrole ALUMINO-SILICATE DOPE CATALYST AND IMPROVED PROCESS FOR TREATING HYDROCARBON LOADS
US8476352B2 (en) * 2008-08-08 2013-07-02 Exxonmobil Chemical Patents Inc. Elastomeric compositions comprising hydrocarbon polymer additives having improved impermeability

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103769125A (en) * 2012-10-24 2014-05-07 中国石油化工股份有限公司 Preparation method of hydro-treatment catalyst
CN104588076A (en) * 2013-11-03 2015-05-06 中国石油化工股份有限公司 Hydrocracking catalyst and preparation method thereof
CN104588082A (en) * 2013-11-03 2015-05-06 中国石油化工股份有限公司 Hydrocracking catalyst preparation method
CN104588086A (en) * 2013-11-03 2015-05-06 中国石油化工股份有限公司 Preparation method of hydrocracking catalyst

Also Published As

Publication number Publication date
CN110038621A (en) 2019-07-23

Similar Documents

Publication Publication Date Title
CN110038620B (en) Process for preparing hydrocracking catalyst
CN109692693B (en) Hydrorefining catalyst and its preparing process
CN110038580B (en) Preparation method of hydrofining catalyst
CN110038622B (en) Hydrocracking catalyst and preparation method thereof
CN110038633B (en) Hydrocracking catalyst and production method thereof
CN110038621B (en) Production method of hydrocracking catalyst
CN110038582B (en) Preparation method of hydrocracking catalyst
CN110038617B (en) Hydrocracking catalyst and preparation method thereof
CN109692685B (en) Preparation method of hydrofining catalyst
CN110038619B (en) Production method of hydrocracking catalyst
CN110038596B (en) Hydrocracking catalyst and production method thereof
CN110038618B (en) Preparation method of hydrocracking catalyst
CN110038584B (en) Process for preparing hydrorefining catalyst
CN110038581B (en) Method for preparing hydrofining catalyst
CN110038625B (en) Method for preparing hydrocracking catalyst
CN110038624B (en) Preparation method of hydrocracking catalyst
CN110041959B (en) Preparation method of hydrocracking catalyst
CN110038623B (en) Hydrocracking catalyst and preparation method thereof
CN111822034B (en) Preparation method of hydrocracking catalyst
CN110038597B (en) Preparation method of hydrofining catalyst
CN109692692B (en) Preparation method of hydrofining catalyst
CN111822038B (en) Preparation method of hydrocracking catalyst
CN111822039B (en) Preparation method of rare earth-containing hydrocracking catalyst
CN109692712B (en) Hydrofining catalyst and preparation method thereof
CN109692686B (en) Hydrofining catalyst and preparation method thereof

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right
TR01 Transfer of patent right

Effective date of registration: 20231012

Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Patentee after: CHINA PETROLEUM & CHEMICAL Corp.

Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd.

Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Patentee before: CHINA PETROLEUM & CHEMICAL Corp.

Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp.