CN110465306B - Preparation method of efficient bulk phase hydrogenation catalyst - Google Patents

Preparation method of efficient bulk phase hydrogenation catalyst Download PDF

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CN110465306B
CN110465306B CN201910713056.4A CN201910713056A CN110465306B CN 110465306 B CN110465306 B CN 110465306B CN 201910713056 A CN201910713056 A CN 201910713056A CN 110465306 B CN110465306 B CN 110465306B
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temperature
containing compound
diatomite
catalyst
hydrogenation catalyst
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CN110465306A (en
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李贺
曾贤君
张利杰
冯晴
孙彦民
于海斌
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CNOOC Energy Technology and Services Ltd
CNOOC Tianjin Chemical Research and Design Institute Co Ltd
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CNOOC Energy Technology and Services Ltd
CNOOC Tianjin Chemical Research and Design Institute Co Ltd
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    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/888—Tungsten
    • B01J23/8885—Tungsten containing also molybdenum
    • B01J35/23—
    • B01J35/393—
    • B01J35/615—
    • B01J35/633—
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0018—Addition of a binding agent or of material, later completely removed among others as result of heat treatment, leaching or washing,(e.g. forming of pores; protective layer, desintegrating by heat)
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • B01J37/10—Heat treatment in the presence of water, e.g. steam
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/20—Sulfiding
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P

Abstract

The invention relates to a preparation method of a high-efficiency bulk phase hydrogenation catalyst, which comprises the following steps: mixing a Ni-containing compound, diatomite, a dispersing agent and deionized water to form a highly dispersed system, then adding a guiding agent to uniformly distribute Ni source particles in a highly dispersed state in a pore structure of a diatomite substrate, then sequentially adding a Mo-containing compound and a W-containing compound to combine with the Ni-containing compound to form a highly dispersed Ni-Mo and Ni-W active phase, then adding diatomite to adsorb soluble metal components in the system, and then filtering slurry to obtain a filter cake; and drying the filter cake properly, extruding, drying and roasting to obtain the catalyst. The catalyst prepared by the method has the advantages of small crystal grain size of the active phase, uniform distribution, good dispersibility, high effective utilization rate of the active phase, excellent pore structure property and better desulfurization effect on high-sulfur poor diesel oil, and the method can also obviously reduce the metal loss rate and the preparation cost, so that the preparation process is more efficient and green.

Description

Preparation method of efficient bulk phase hydrogenation catalyst
Technical Field
The invention belongs to the field of preparation of petrochemical hydrogenation catalysts, relates to a preparation method of a high-efficiency bulk phase hydrogenation catalyst, and particularly relates to a preparation method of a high-activity catalyst suitable for deep hydrogenation of inferior distillate oil.
Background
Petroleum is the blood of the contemporary industry and is the source of economic development and social progress. In recent years, with the rapid development of science and technology and the continuous improvement of the living demands of people on substances, the consumption of petroleum is increased year by year in astonishing numbers, the continuous exploitation makes the crude oil be more inferior, the processing difficulty is gradually increased, the contents of sulfur, nitrogen and aromatic hydrocarbon of oil products such as gasoline, diesel oil and the like are increased, the service performance is reduced, and the combustion of high-sulfur high-nitrogen low-quality oil products emits a large amount of toxic and harmful sulfur, nitrogen oxides and particle pollutants to the environment, so that the atmospheric pollution caused by the emission brings great threats to the living environment and the body health of people. In order to solve the problem, relevant laws and regulations are issued in various countries and regions in the world to limit the emission of pollutants in the tail gas of automobiles, as early as 2009, the European Union has implemented the 'European five' emission standard that the sulfur content of gasoline and diesel oil for automobiles is not higher than 10ppm, in 2013, the stricter 'European six' emission standard is implemented, and China is expected to implement the 'national six' emission standard which is equal to the 'European six' in 2020. Therefore, the development of the production process of ultra-clean oil products is imperative.
At present, hydrogenation is the most effective process means for realizing oil product cleanness and is widely applied at home and abroad, and a hydrogenation catalyst is the core technology of a hydrogenation process and is the key for rapidly finishing quality upgrading of oil products. In order to adapt to the continuously improved emission standard, workers in related fields at home and abroad strive to continuously improve the performance of a hydrogenation catalyst, and the catalyst with ultra-deep hydrorefining performance, which can effectively realize the production of ultra-clean oil products, becomes the main research and development target of researchers. The traditional hydrogenation catalyst is a supported catalyst and mainly comprises active components containing VIB group and VIII group metals and a carrier taking alumina and a molecular sieve as main components. CN104258895A is a hydrofining catalyst which takes porous materials such as pseudo-boehmite and the like as a carrier, takes molybdenum or tungsten sulfide as an active component and takes transition metal sulfide as an auxiliary agent to prepare molybdenum or tungsten sulfide with the mass of 8-60 wt%, the auxiliary agent of 1-25 wt% and the balance of carrier; US4330395 discloses a process for preparing a catalyst for hydrorefining middle distillate, which comprises the steps of hydro-thermal synthesis of tungsten-containing compounds and aluminum-containing compounds, drying, calcining, impregnating with a solution containing nickel compounds, and finally sulfurizing and fluorinating with sulfur-containing compounds and fluorine-containing compounds; CN1470610A takes alumina and cation-exchanged zeolite as carriers, sequentially impregnates the carriers with aqueous solution of precursors containing nickel, molybdenum and phosphorus, and prepares the catalyst for hydrorefining of middle distillate oil, wherein the weight of nickel oxide is 2.5-8 wt%, the weight of molybdenum oxide is 10-30 wt% and the weight of phosphorus is 0.2-4 wt%.
Although the supported hydrogenation catalyst is a main kind of the current industrial hydrogenation catalyst, because the loading capacity of the active component is limited, the hydrogenation activity is limited, and the requirement of ultra-deep hydrofining of inferior oil products is difficult to meet, the research and development of a novel catalyst with higher hydrogenation activity is favored by researchers. The bulk phase hydrogenation catalyst is a hydrogenation catalyst which is developed in recent years, has higher hydrogenation activity than a supported catalyst, can effectively realize ultra-deep hydrogenation refining of diesel oil and other oil products, and among various bulk phase hydrogenation catalysts, the bulk phase NiMoW hydrogenation catalyst shows the most excellent hydrogenation performance. The bulk phase catalyst is a catalyst with high activity, which is prepared by synthesizing catalyst particles with excellent pore channel structures through reaction and then adding an auxiliary agent for molding. US2002010088A and US2003102254A prepared a NiMoW mixed metal compound by hydrothermal synthesis and formed to prepare a bulk hydrogenation catalyst. CN101153228A discloses a method for preparing a bulk NiMoW hydrogenation catalyst by a hydrothermal method, wherein the prepared catalyst has a smaller particle size and higher hydrogenation activity. CN106179390A firstly makes the mixed component containing W, Ni and Al undergo the process of gelatinizing reaction, after filtering it and MoO3Pulping, mixing, filtering, washing, molding, drying and roasting to obtain the bulk NiMoW hydrofining catalyst.
The hydrothermal synthesis method is still the mainstream preparation method of the bulk NiMoW hydrogenation catalyst at present, and although the catalyst prepared by the hydrothermal method has higher hydrogenation activity, the preparation method has the following defects: (1) the active phase is easy to agglomerate, so that the effective utilization rate of the active phase is insufficient; (2) part of active metal remains in the tail liquid of the synthesis reaction, so that the loss of the active metal is caused, and the difficulty in treating the tail liquid is increased; (3) the molding process is complex and the catalyst preparation cost is high.
Some researchers have improved the preparation of bulk NiMoW hydrogenation catalysts based on hydrothermal synthesis. CN103240096A takes the tail liquid of NiMoW composite oxide as the solvent of the next synthesis reaction, and realizes the recycling of the tail liquid, although the method reduces the discharge of the tail liquid, the reaction tail liquid always contains the active metal which is not recycled, and the metal utilization rate is insufficient; in the preparation method of the bulk NiMoW hydrogenation catalyst disclosed in CN101296747A, a synthesized NiMoW active precursor filter cake and dry powder of a binder (an inactive substance serving as a catalyst substrate) are directly mixed and then formed, the method simplifies the preparation process of the catalyst, and omits the steps of drying and crushing the filter cake, adding additional water and kneading the binder and the like, but the filter cake and the dry powder of the binder are difficult to be uniformly mixed, so that the problems of uneven catalyst activity and mechanical strength and the like are easily caused; CN108067246A firstly adds Ni, Mo, W metal salt and reaction auxiliary agent into a reaction container, adds aluminum hydroxide dry glue after hydrothermal reaction, and after aging, the bulk NiMoW hydrogenation catalyst is prepared through the steps of pumping filtration, washing, drying, forming, roasting and the like.
Although the method optimizes and improves the preparation of the bulk NiMoW hydrogenation catalyst based on the hydrothermal synthesis method in some aspects, the three problems existing in the preparation process are difficult to be solved comprehensively.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects of the prior art and provide a preparation method of a high-efficiency bulk phase hydrofining catalyst, the method is based on a hydrothermal synthesis method, and aiming at a bulk phase NiMoW hydrogenation catalyst, the agglomeration of Ni-Mo and Ni-W active phases is obviously reduced, so that the active phases are uniformly distributed on a binder matrix in a highly dispersed state, the pore structure property of the catalyst is improved, and the effective utilization rate of the active phases is improved; in addition, the preparation method reduces the content of metal ions in the hydrothermal reaction tail liquid, reduces the treatment difficulty of the tail liquid and the loss rate of active metals, and improves the hydrodesulfurization activity of the catalyst; in addition, the preparation method adds all the binders in the synthesis reaction stage, simplifies the catalyst forming process and reduces the catalyst cost.
The invention relates to a preparation method of a high-efficiency bulk phase hydrofining catalyst, which comprises the following steps:
(1) preparation of reactive precursors
Uniformly mixing a Ni-containing compound, kieselguhr, a dispersing agent and deionized water, adding the mixture into a high-pressure reaction kettle, heating the mixture to 60-100 ℃ under mechanical stirring, preferably 70-90 ℃, keeping the temperature constant for 1-5 hours, then adding a guiding agent, reducing the stirring speed, raising the temperature of the system to 100-180 ℃, preferably 120-160 ℃, keeping the temperature constant for 1-3 hours, adding a Mo-containing compound, dropwise adding ammonia water, keeping the temperature constant for 1-4 hours, then adding a W-containing compound, adjusting the pH of the system to 4-5, reacting at constant temperature for 1-4 hours, preferably 2-3 hours, then adding kieselguhr, keeping the temperature constant for 1-3 hours, closing the heating, cooling the system to room temperature, collecting slurry, and filtering the slurry to obtain a mixture filter cake of an active precursor and a binder;
the molar ratio of Ni, Mo and W in the active precursor is (1-3) to (1-2); the total adding amount of the diatomite is 10-60 wt%, preferably 20-50 wt% of the total amount of the metal oxides of Ni, Mo and W; the specific surface area of the diatomite is not less than 60m2Per g, pore volume is not less than 0.6cm3/g；
(2) Shaping of the catalyst
And drying the active precursor filter cake until the water content is 10-20 wt%, adding the active precursor filter cake into a kneader to perform extrusion molding, drying the extrudate at 80-120 ℃ for 8-12 h, and roasting at 350-450 ℃ for 3-7 h to obtain the bulk phase hydrogenation catalyst.
(3) Presulfiding of catalysts
In the step (2), the catalyst can play a better hydrogenation role only by being subjected to pre-vulcanization treatment, wherein the vulcanization temperature is 300-400 ℃, the preferable vulcanization time is 330-370 ℃, the vulcanization time is 8-16 h, the preferable vulcanization time is 10-14 h, and the volume ratio of hydrogen to oil is 400-800, and the preferable vulcanization time is 500-700.
The Ni-containing compound is basic nickel carbonate or nickel acetate, and the Mo-containing compound is ammonium molybdate or molybdenum trioxide.
The dispersing agent is one or more of polyvinyl alcohol 17-92, polyvinylpyrrolidone and polyethylene glycol 2000.
The guiding agent is one or more of isopropylamine, diisopropylamine, triethanolamine and triisopropanolamine.
The adding proportion of the diatomite in the two times is (3:1) - (5: 1).
The bulk NiMoW hydrogenation catalyst prepared by the conventional hydrothermal method has the advantages of easy agglomeration of active phases, insufficient utilization rate of active metals and complex forming process, thereby increasing the preparation cost of the catalyst. The method of the invention is characterized in that:
1) the hydrothermal reaction stage comprises the steps of firstly, simultaneously adding part of diatomite with a developed pore channel structure as a binder, a Ni source as an active phase crystallization center and a dispersing agent into a reaction system, under the comprehensive action of mechanical stirring and the dispersing agent, enabling the diatomite and the Ni source to be in a highly dispersed and independently existing small particle state, then adding a guiding agent, under the adsorption action of the guiding agent and the diatomite, enabling Ni source particles to be uniformly distributed in the pore channel structure of a diatomite substrate in a highly dispersed state, realizing the physical combination of the diatomite and the diatomite, then sequentially adding a Mo source and a W source, combining with the highly dispersed Ni source to form Ni-Mo and Ni-W active phases, then adding the rest diatomite, adsorbing soluble metal components in the system, finally filtering reaction slurry to obtain a mixture filter cake of an active precursor and the binder, and fully utilizing the developed pore channel structure of the diatomite in the preparation stage, the agglomeration of Ni-Mo or Ni-W active phase is obviously reduced, the pore structure property of the catalyst is improved, the effective utilization rate of the active phase is improved, in addition, the diatomite adsorbs soluble active metal in the slurry, the loss rate of the active metal and the treatment difficulty of tail liquid are reduced, and the hydrogenation activity of the catalyst is improved.
2) The diatomite as the binder is completely added into the liquid phase system and forms a highly homogenized system with the active precursor under the comprehensive action of full stirring and the dispersing agent, so that the phenomenon of uneven mixing possibly caused by mixing the binder with the active precursor in a dry powder form in the traditional preparation method is avoided, and the property of the catalyst is more uniform and stable.
3) And in the catalyst forming stage, the filter cake after reaction slurry filtration can be extruded and formed after being properly dried, and compared with the traditional dry mixing method, the steps of crushing the dried filter cake, fully mixing with binder powder, adding water for kneading and the like are omitted, the forming process flow is greatly simplified, and the catalyst cost is reduced.
Drawings
FIG. 1 is a Scanning Electron Microscope (SEM) image of the catalyst of example 1;
fig. 2 is a Scanning Electron Microscope (SEM) image of the catalyst of comparative example 6.
Detailed Description
Example 1
50g of basic nickel carbonate and 58g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3Uniformly mixing 17-92 g of polyvinyl alcohol and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 rpm, heating the mixture to 80 ℃, keeping the temperature constant for 3 hours, then adding 3g of diisopropylamine, reducing the stirring speed to 200 rpm, raising the system temperature to 140 ℃, keeping the temperature constant for 2 hours, adding 53g of ammonium molybdate, then dropwise adding 10ml of 25 wt% ammonia water into the system, keeping the temperature constant for 2 hours, then adding 79.2g of ammonium metatungstate, then adding citric acid until the system pH is 4.2, keeping the temperature constant for 3 hours, and then adding 15g of diatomite (the specific surface area is 78 m)2Per g, pore volume 0.65cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; and drying the filter cake until the water content is 15%, adding the filter cake into a kneader to extrude and mold, obtaining a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting the strip in a muffle furnace at 400 ℃ for 5h to obtain the bulk phase hydrogenation catalyst, which is marked as CAT-1.
Example 2
50g of basic nickel carbonate and 58g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3Uniformly mixing 5g of polyethylene glycol 2000 and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 rpm, heating the mixture to 80 ℃, keeping the temperature for 3 hours, adding 4g of triethanolamine, reducing the stirring speed to 200 rpm, raising the system temperature to 140 ℃, keeping the temperature constantAfter 2 hours, 53g of ammonium molybdate was added, 10ml of 25 wt% ammonia water was added dropwise to the system, the temperature was kept constant for 2 hours, 79.2g of ammonium metatungstate was added, citric acid was added until the pH of the system was 4.2, and after 3 hours, 15g of diatomaceous earth (with a specific surface area of 78 m) was added2Per g, pore volume 0.65cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; and drying the filter cake until the water content is 15%, adding the filter cake into a kneader to extrude and mold, obtaining a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting the strip in a muffle furnace at 400 ℃ for 5h to obtain the bulk phase hydrogenation catalyst, which is marked as CAT-2.
Example 3
88.6g of nickel acetate and 58g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3Uniformly mixing 17-92 g of polyvinyl alcohol and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 rpm, heating the mixture to 80 ℃, keeping the temperature constant for 3 hours, then adding 3g of diisopropylamine, reducing the stirring speed to 200 rpm, raising the system temperature to 140 ℃, keeping the temperature constant for 2 hours, adding 43.2g of molybdenum trioxide, then dropwise adding 10ml of 25 wt% ammonia water into the system, keeping the temperature constant for 2 hours, then adding 79.2g of ammonium metatungstate, then adding citric acid until the system pH is 4.2, keeping the temperature constant for 3 hours, then adding 15g of diatomite (the specific surface area is 78 m)2Per g, pore volume 0.65cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; and drying the filter cake until the water content is 15%, adding the filter cake into a kneader to extrude and mold, obtaining a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting the strip in a muffle furnace at 400 ℃ for 5h to obtain the bulk phase hydrogenation catalyst, which is marked as CAT-3.
Comparative example 1
50g of basic nickel carbonate and 58g of diatomaceous earth (specific surface area 42 m)2G, pore volume 0.39cm3Uniformly mixing the mixture of the polyvinyl alcohol 17-92 g and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 rpm, heating the mixture to 80 ℃, keeping the temperature for 3 hours, and then carrying outAdding 3g of diisopropylamine, reducing the stirring speed to 200 r/min, raising the temperature of the system to 140 ℃, keeping the temperature constant for 2h, adding 53g of ammonium molybdate, then dropwise adding 10ml of 25 wt% ammonia water into the system, keeping the temperature constant for 2h, then adding 79.2g of ammonium metatungstate, then adding citric acid until the pH value of the system is 4.2, keeping the temperature constant for 3h, and then adding 15g of diatomite (the specific surface area is 42 m)2G, pore volume 0.39cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; and drying the filter cake until the water content is 15%, adding the filter cake into a kneader to extrude and mold, obtaining a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting the strip in a muffle furnace at 400 ℃ for 5h to obtain the bulk phase hydrogenation catalyst, which is marked as CAT-4.
Comparative example 2
50g of basic nickel carbonate and 58g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3/g) is evenly mixed with 600ml of deionized water and then added into a 2L high-pressure reaction kettle, the stirring speed is set to 400 r/min, the mixture is heated to 80 ℃, the temperature is kept constant for 3h, then 3g of diisopropylamine is added, the stirring speed is reduced to 200 r/min, the system temperature is raised to 140 ℃, 53g of ammonium molybdate is added after the temperature is kept constant for 2h, then 10ml of 25 wt% ammonia water is added into the system dropwise, the temperature is kept constant for 2h, 79.2g of ammonium metatungstate is added, then citric acid is added until the system pH is 4.2, and after the temperature is kept constant for 3h, 15g of diatomite (the specific surface area is 78 m)2Per g, pore volume 0.65cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; and drying the filter cake until the water content is 15%, adding the filter cake into a kneader to extrude and mold, obtaining a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting the strip in a muffle furnace at 400 ℃ for 5h to obtain the bulk phase hydrogenation catalyst, which is marked as CAT-5.
Comparative example 3
Uniformly mixing 50g of basic nickel carbonate, 4g of polyvinyl alcohol 17-92 and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 rpm, heating the mixture to 80 ℃, keeping the temperature for 3 hours, and then increasing the temperatureHeating the system to 140 ℃, adding 53g of ammonium molybdate, then dropwise adding 10ml of 25 wt% ammonia water into the system, keeping the temperature constant for 2 hours, then adding 79.2g of ammonium metatungstate, then adding citric acid until the pH value of the system is 4.2, keeping the temperature constant for 3 hours, and then adding 73g of diatomite (with the specific surface area of 78 m)2Per g, pore volume 0.65cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; and drying the filter cake until the water content is 15%, adding the filter cake into a kneader to extrude and mold, obtaining a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting the strip in a muffle furnace at 400 ℃ for 5h to obtain the bulk phase hydrogenation catalyst, which is marked as CAT-6.
Comparative example 4
50g of basic nickel carbonate and 58g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3Uniformly mixing 17-92 g of polyvinyl alcohol and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 r/m, heating the mixture to 80 ℃, keeping the temperature constant for 3h, then adding 3g of diisopropylamine, reducing the stirring speed to 200 r/m, raising the temperature of the system to 140 ℃, keeping the temperature constant for 2h, adding 53g of ammonium molybdate, then dropwise adding 10ml of 25 wt% ammonia water into the system, keeping the temperature constant for 2h, then adding 79.2g of ammonium metatungstate, then adding citric acid until the pH value of the system is 4.2, keeping the temperature constant for 3h, then closing and heating, cooling the system to room temperature, closing and stirring, collecting slurry, and performing suction filtration on the slurry to obtain a mixture of an active precursor and diatomite; the filter cake was mixed with 15g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3And/g) fully kneading, adding into a kneader, extruding and molding to obtain a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting in a muffle furnace at 400 ℃ for 5h to obtain the bulk hydrogenation catalyst, which is marked as CAT-7.
Comparative example 5
Uniformly mixing 50g of basic nickel carbonate, 4g of polyvinyl alcohol 17-92 and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 rpm, heating the mixture to 80 ℃, keeping the temperature for 3 hours, raising the system temperature to 140 ℃, adding 53g of ammonium molybdate, and then dropwise adding 10ml of 25 wt% ammonia waterAdding into the system, keeping constant temperature for 2h, adding 79.2g ammonium metatungstate, adding citric acid until pH is 4.2, keeping constant temperature for 3h, adding 58g diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3The temperature is kept constant for 1 hour, the heating is closed, the stirring is closed after the system is cooled to the room temperature, slurry is collected, and the slurry is filtered to obtain a mixture filter cake of the active precursor and the diatomite; the filter cake was mixed with 15g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3And/g) fully kneading, adding into a kneader, extruding and molding to obtain a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting in a muffle furnace at 400 ℃ for 5h to obtain the bulk hydrogenation catalyst, which is marked as CAT-8.
Comparative example 6
Uniformly mixing 50g of basic nickel carbonate, 4g of polyvinyl alcohol 17-92 and 600ml of deionized water, adding the mixture into a 2L high-pressure reaction kettle, setting the stirring speed to 400 revolutions per minute, heating the mixture to 80 ℃, keeping the temperature constant for 3 hours, then raising the temperature of the system to 140 ℃, adding 53g of ammonium molybdate, then dropwise adding 10ml of 25 wt% ammonia water into the system, keeping the temperature constant for 2 hours, adding 79.2g of ammonium metatungstate, then adding citric acid until the pH value of the system is 4.2, keeping the temperature constant for 3 hours, then stopping heating, cooling the system to room temperature, stopping stirring, collecting slurry, and performing suction filtration on the slurry to obtain a mixture filter cake of an active precursor and diatomite; the filter cake was mixed with 73g of diatomaceous earth (specific surface area 78 m)2Per g, pore volume 0.65cm3And/g) fully kneading, adding into a kneader, extruding and molding to obtain a strip with the diameter of 1.5mm, drying the strip at 110 ℃ for 10h, and roasting in a muffle furnace at 400 ℃ for 5h to obtain the bulk hydrogenation catalyst, which is marked as CAT-9.
TABLE 1 structural Properties of the catalysts and Synthesis tailrace Metal ratios
Figure BDA0002154434270000071
Catalyst evaluation method
The evaluation of the activity of the catalyst is carried out on a 20ml high-pressure micro-reactor, the catalyst is filled into a reactor, 3 wt% of CS is pumped when the temperature of the reactor is raised to 120 DEG C2-cyclohexane solutionPre-vulcanizing, heating to 350 ℃, vulcanizing for 12h, and keeping the liquid hourly space velocity of 2h-1Hydrogen to oil volume ratio 600. After the vulcanization is finished, the activity of the catalyst is evaluated by taking high-sulfur poor diesel oil with the sulfur content of 11000 mu g/g and the density of 0.8906g/ml as a raw material, and the reaction conditions are as follows: the reaction temperature is 350 ℃, the reaction pressure is 6MPa, and the liquid hourly space velocity is 2h-1And a hydrogen-oil volume ratio of 500. The results of the activity evaluation of the catalyst are shown in Table 2.
TABLE 2 evaluation results of catalyst Activity
Figure BDA0002154434270000072
Figure BDA0002154434270000081
The data in Table 1 show that the catalysts (CAT-1, 2 and 3) prepared by the method have smaller grain sizes of Ni-Mo and Ni-W active phases, and the specific surface area and the pore volume of the catalysts are larger, which indicates that the active phases have good dispersibility, low agglomeration degree and more contact opportunities with reactant molecules, and the effective utilization rate of the active phases is improved; in addition, as shown in table 1, the hydrothermal reaction tail liquid of the method of the present invention has a low metal content, which indicates that the raw material utilization rate is improved, and the tail liquid treatment difficulty is reduced, which is beneficial to improving the catalyst activity and reducing the catalyst preparation cost. FIG. 1 is SEM images of a catalyst prepared by the method of the present invention and a catalyst prepared by kneading and molding a dry binder powder and an active precursor filter cake, and it can be seen that particles in the catalyst prepared by the method of the present invention are uniformly distributed in a smaller size, thereby avoiding the phenomena of difficult uniform dispersion and easy occurrence of large particle aggregation between the active precursor and the binder in the conventional method, and providing an excellent pore structure for the hydrogenation reaction; in addition, compared with the traditional method, the method of the invention can greatly simplify the catalyst forming process and reduce the preparation cost of the catalyst. The data in Table 2 show that the catalyst prepared by the method has stronger removal capability to sulfur in high-sulfur poor diesel oil, and can achieve better desulfurization effect under the same reaction condition compared with the catalyst prepared by the traditional method. The method can effectively improve the activity of the bulk phase hydrogenation catalyst, reduce the cost of the catalyst, lead the preparation process to be more green and fully embody the high efficiency of the bulk phase hydrogenation catalyst.

Claims (8)

1. A preparation method of a high-efficiency bulk phase hydrogenation catalyst is characterized by comprising the following steps:
(1) preparation of reactive precursors
Uniformly mixing a Ni-containing compound, kieselguhr, a dispersing agent and deionized water, adding the mixture into a high-pressure reaction kettle, heating the mixture to 60-100 ℃ under mechanical stirring, keeping the temperature constant for 1-5 hours, adding a guiding agent, reducing the stirring speed, raising the temperature of the system to 100-180 ℃, keeping the temperature constant for 1-3 hours, adding a Mo-containing compound, dropwise adding ammonia water, keeping the temperature constant for 1-4 hours, adding a W-containing compound and a reaction auxiliary agent, adjusting the pH of the system to 4-5, reacting at constant temperature for 1-4 hours, adding kieselguhr, keeping the temperature constant for 1-3 hours, stopping heating, cooling the system to room temperature, collecting slurry, and filtering the slurry to obtain an active precursor filter cake; the molar ratio of Ni, Mo and W in the active precursor is (1-3) to (1-2); the total amount of the diatomite added twice is 10-60 wt% of the total amount of Ni, Mo and W metal oxides;
(2) shaping of the catalyst
Drying the active precursor filter cake until the water content is 10-20 wt%, adding the active precursor filter cake into a kneader to perform extrusion molding, drying an extruded product at the temperature of 80-120 ℃ for 8-12 h, and roasting at the temperature of 350-450 ℃ for 3-7 h to obtain a bulk phase hydrogenation catalyst;
(3) presulfiding of catalysts
Pre-vulcanizing the bulk phase hydrogenation catalyst obtained in the step (2) at the temperature of 300-400 ℃ for 8-16 h, and controlling the volume ratio of hydrogen to oil to be 400-800;
the specific surface area of the diatomite is not less than 60m2Per g, pore volume is not less than 0.6cm3/g。
2. The method according to claim 1, wherein the Ni-containing compound is basic nickel carbonate or nickel acetate, and the Mo-containing compound is ammonium molybdate or molybdenum trioxide.
3. The method for preparing a high efficiency bulk phase hydrogenation catalyst according to claim 1, wherein the dispersant is one or more of polyvinyl alcohol 17-92, polyvinylpyrrolidone, and polyethylene glycol 2000.
4. The method as claimed in claim 1, wherein the guiding agent is one or more selected from isopropylamine, diisopropylamine, triethanolamine, and triisopropanolamine.
5. The method according to claim 1, wherein the ratio of the diatomaceous earth added in the first and second steps is (3:1) - (5: 1).
6. The preparation method of the efficient bulk phase hydrogenation catalyst according to claim 1, wherein the Ni-containing compound, the diatomite, the dispersant and the deionized water are uniformly mixed and then added into a high-pressure reaction kettle, the mixture is heated to 70-90 ℃ under mechanical stirring, the temperature is kept constant for 1-5 h, the guiding agent is added, the stirring speed is reduced, the system temperature is increased to 120-160 ℃, the temperature is kept constant for 1-3 h, the Mo-containing compound is added, then ammonia water is added dropwise, the temperature is kept constant for 1-4 h, the W-containing compound is added, the pH of the system is adjusted to 4-5, the diatomite is added after the constant temperature reaction is carried out for 2-3 h, the heating is stopped after the temperature is kept constant for 1-3 h, the slurry is collected after the system is cooled to the room temperature, and the slurry is filtered to obtain the active precursor filter cake.
7. The method as claimed in claim 1, wherein the total amount of the diatomite added twice is 20-50 wt% of the total amount of the Ni, Mo and W metal oxides.
8. The preparation method of the high-efficiency bulk phase hydrogenation catalyst according to claim 1, wherein the bulk phase hydrogenation catalyst in the step (3) is subjected to sulfidation treatment at 330-370 ℃ for 10-14 h, and the volume ratio of hydrogen to oil is 500-700.
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