CN109382136B - Gaseous hydrocarbon steam conversion upper-section catalyst and preparation method thereof - Google Patents

Gaseous hydrocarbon steam conversion upper-section catalyst and preparation method thereof Download PDF

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CN109382136B
CN109382136B CN201710652492.6A CN201710652492A CN109382136B CN 109382136 B CN109382136 B CN 109382136B CN 201710652492 A CN201710652492 A CN 201710652492A CN 109382136 B CN109382136 B CN 109382136B
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catalyst
carrier
gaseous hydrocarbon
rare earth
roasting
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CN109382136A (en
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王昊
白志敏
何宗华
薛红霞
姜建波
齐焕东
宋晓军
梁卫忠
徐保民
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China Petroleum and Chemical Corp
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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
    • 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
    • B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
    • B01J29/14—Iron group metals or copper
    • B01J29/146—Y-type faujasite
    • 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
    • B01J37/082—Decomposition and pyrolysis
    • B01J37/088—Decomposition of a metal salt
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/40—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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Abstract

The invention belongs to the technical field of hydrocarbon steam conversion, and particularly relates to a gaseous hydrocarbon steam conversion upper-section catalyst and a preparation method thereof. The catalyst takes nickel and rare earth as active components, the content of NiO in the catalyst is 5-25 wt.%, and the content of rare earth metal oxide is 0.3-15 wt.%; loading active components of nickel and rare earth on a carrier by adopting a co-impregnation method; the preparation method of the carrier comprises the following steps: (1) FCC catalyst waste treatment: roasting the FCC catalyst waste agent in an air atmosphere, crushing and sieving to obtain powder; (2) preparing a carrier: mixing the powder, magnesium oxide, an anti-carbon auxiliary agent, a pore-forming agent, a lubricant and a binder, performing ball milling, kneading, granulating and extrusion forming to obtain a raw ring, and performing maintenance, drying and roasting to obtain the carrier. The catalyst has good carbon resistance, mechanical strength and conversion activity, and is matched with a lower catalyst to prepare hydrogen or carbonyl synthesis gas; the preparation method has simple process and low cost.

Description

Gaseous hydrocarbon steam conversion upper-section catalyst and preparation method thereof
Technical Field
The invention belongs to the technical field of hydrocarbon steam conversion, and particularly relates to a gaseous hydrocarbon steam conversion upper-section catalyst and a preparation method thereof.
Background
Hydrocarbon steam conversion is a commonly adopted hydrogen production method in domestic and overseas refining enterprises at present.
In the past, naphtha was used as a main raw material for hydrocarbon steam reforming, and due to the greatly increased price of light naphtha, gaseous hydrocarbons such as natural gas and the like which are relatively cheap are used as hydrogen production raw materials as much as possible abroad, so that the hydrogen cost is reduced. However, for most domestic oil refining chemical enterprises which lack natural gas resources, LPG, propane, naphtha and the like are still used as hydrogen production raw materials. With the progress of hydrogen production technology and the increasing demand of hydrogen, the relatively cheap refinery gas resources of refineries are more and more paid attention. Hydrogen production plants have also increased year by treating various refinery-related gases separately, either alone or with liquid hydrocarbons, as the hydrogen production feedstock. The light hydrocarbon such as refinery gas is used as raw material, so that the production cost of industrial hydrogen is greatly reduced, and the operation condition of the converter is obviously improved. Mainly characterized in that the carbon deposition tendency of the light hydrocarbon raw material is obviously reduced, and the operation safety of the industrial device is improved. Based on the new characteristics of the current hydrogen production raw materials and the defects of the existing catalyst in the aspect of steam conversion of refinery gas and hydrocarbons, ZL 102451696 discloses a catalyst for the reaction of preparing hydrogen or oxo synthesis gas by steam conversion of hydrocarbons, which has good industrial application effect but high production cost.
Refinery catalytic cracking (FCC) catalyst is the most used catalyst in refinery processes, and as the scale of FCC increases, the amount of spent catalyst exceeds 10 million tons per year, which is not only an economic problem but also more important an environmental problem. The FCC spent is composed mainly of Al2O3、SiO2Clay and BaCO3The waste agent of the type prepared by mixing has low activity and contains a certain amount of heavy metal, and how to treat the waste agent is one of the subjects concerned by the industry. At present, the method with more success is to recycle the waste agent part and reduce the amount of disposal treatment, and the method mainly comprises the steps of recycling by a magnetic separation technology, using as a cement substitute material, using as a flame retardant and a microorganism growth inhibitor, recrystallizing into a catalyst and the like. However, these treatments have the following drawbacks: 1. the treatment cost is high; 2. the waste dosage is less. Landfilling is the most cost effective way, but can cause great harm to the environment.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide an upper catalyst for gaseous hydrocarbon steam reforming, which has good carbon resistance, mechanical strength and reforming activity and is matched with a lower catalyst for preparing hydrogen or oxo-synthesis gas; the invention also provides a preparation method of the composite material, which has simple process and low preparation cost.
The upper-section catalyst for gaseous hydrocarbon steam reforming takes nickel and rare earth as active components, and in the catalyst, the content of NiO is 5-25 wt%, and the content of rare earth metal oxide is 0.3-15 wt%; loading active components of nickel and rare earth on a carrier by adopting a co-impregnation method;
the carrier is prepared by the following method:
(1) FCC catalyst waste treatment:
roasting the FCC catalyst waste agent in an air atmosphere, crushing and sieving to obtain powder;
(2) preparing a carrier:
mixing powder, magnesium oxide, an anti-carbon auxiliary agent, a pore-forming agent, a lubricant and a binder, wherein the mixing mass ratio is 100: 25-200: 20-100: 1-5: 1-5: 30-120, then performing ball milling, kneading, granulating, extrusion forming to obtain a raw ring, and performing curing, drying and roasting to obtain the carrier.
In the catalyst, the content of NiO is 8-17 wt.%, and the content of rare earth metal oxide is 0.5-12 wt.%.
In the catalyst, the content of NiO is 5-25 wt.%, preferably 8-17 wt.%; the content of the rare earth metal oxide is 0.3-15 wt.%, preferably 0.5-12 wt.%; the sum of the oxide contents of the alkaline earth metals is 4-50 wt.%, wherein the content of magnesium oxide is 4-30 wt.%, preferably 12-25 wt.%; the balance being carriers.
The carrier comprises 10-30% of cement, 5-20% of kaliophilite and the balance of aluminum and silicon by taking the total amount of the carrier as 100%.
The pore volume of the carrier is 0.18-0.22 mL/g, and the pore crushing strength is more than 220N per particle. The water absorption rate of the carrier is 18-22%.
In the step (1), the waste FCC catalyst is prepared from ultrastable Y-type zeolite.
Al as a support component in FCC catalysts2O3And SiO2The content can reach about 95 percent (w), and the microstructure of the catalyst is relatively stable after long-term use. In addition, the waste agent contains partial nickel, so that the possibility of preparing the steam reforming catalyst by using the FCC waste agent as a raw material is provided. Meanwhile, the steam conversion catalyst prepared by taking the FCC waste agent as the raw material not only can reduce the preparation cost and improve the competitive strength, but also can find an effective utilization way for the FCC waste agent with wide source and low cost, and relieve the huge pressure of the treatment of the FCC waste agent on the ecological environment.
In the step (1), the roasting temperature is 500-700 ℃, and the roasting time is 2-10 h. The roasting temperature is preferably 600 ℃, and the roasting time is preferably 3-4 h.
In the step (1), the sieving is carried out by a 280-320 mesh sieve, preferably a 320 mesh sieve.
In the step (2), the magnesium oxide is one or a mixture of two of light magnesium oxide and heavy magnesium oxide.
In the step (2), the anti-carbon auxiliary agent is artificially synthesized kaliophilite. The pore-forming agent is graphite, stearic acid, stearate, nitric acid, gamma-Al2O3And one or more of cellulose or plant fiber, preferably graphite and plant fiber. The lubricant is graphite, stearic acid or stearate, preferably graphite. The binder is pure clinker portland cement, preferably 525 cement or 625 cement.
In the step (2), the curing is soaking in water for curing for 24-36 h.
In the step (2), the crushing strength of the green ring after curing is more than 80N/particle, preferably more than 100N/particle.
In the step (2), the roasting temperature is 1200-1300 ℃, and the roasting time is 2-6 hours.
The preparation method of the upper-stage catalyst for the steam reforming of the gaseous hydrocarbon comprises the following steps:
loading active components of nickel and rare earth on a carrier by adopting a co-impregnation method, wherein the impregnation time is 0.5-6 hours, decomposing at the temperature of 400-700 ℃ for 1-6 hours after drying, and then repeating impregnation, drying and decomposition once to obtain a catalyst finished product.
The carrier of the invention can detect the magnesium aluminum silicate component (cordierite) through XRD analysis.
The pore distribution of the catalyst of the present invention is divided into 2 types: the number of pores with the pore size of 10-15 nm accounts for 35-45% of the total pore volume, and the number of macropores with the pore size of 150-200 nm accounts for 15-25% of the total pore volume.
The catalyst of the invention has the appearance of Raschig rings, four-hole rings, seven-hole rings and the like, and has the same geometric shape and similar size with the existing industrialized hydrocarbon steam reforming catalyst.
Compared with the prior art, the invention has the following beneficial effects:
1. the carrier raw material of the catalyst adopts FCC waste agent with wide source and low cost, greatly reduces the preparation cost of the catalyst, finds an effective way for the comprehensive utilization of the FCC waste agent, effectively relieves the huge pressure of the FCC waste agent on the ecological environment, and has good economic benefit and social benefit.
2. The upper catalyst for gaseous hydrocarbon steam conversion prepared by the invention has good physical and chemical properties and good mechanical strength, and the crushing strength of the catalyst can reach more than 220N per particle.
3. The catalyst adopts potash as a carbon-resistant component, so that the carbon resistance is similar to that of a common bonding catalyst; in addition, the potash is added before the carrier is sintered, and after high-temperature sintering, the mechanical strength and the conversion activity of the potash are similar to those of a common presintering catalyst, and the potash is superior to a cement bonding catalyst.
4. The upper catalyst for converting the gaseous hydrocarbon steam is suitable for the conditions that the inlet temperature of a converter is 450-630 ℃ and the outlet temperature is 700-950 ℃; space velocity of converted carbon<2000h-1(ii) a The water-carbon ratio is 2.5-7.0; the upper catalyst under the process conditions of hydrogen production and oxo-synthesis gas production with the pressure of 1.5-4.0 MPa is matched with the lower catalyst to produce hydrogen or oxo-synthesis gas. The conversion catalyst has stable activity, and the conversion outlet methane meets the process requirements.
5. The preparation method has the advantages of simple process and low preparation cost.
Drawings
FIG. 1 is a diagram of a small-sized pressurized activity evaluation apparatus;
in the figure: 1-oil metering pump; 2-a water metering pump; 3-a vaporizer; 4-a mixer; 5-a tubular reactor; 6-a condenser; 7-a separator; 8, a voltage stabilizer; 9-wet type flowmeter.
Detailed Description
The present invention will be further described with reference to the following examples.
The FCC spent used in the examples was spent on catalysts prepared from ultrastable Y-zeolite.
Example 1
And roasting the FCC waste agent in an air atmosphere at the roasting temperature of 700 ℃ for 2 hours, and crushing the roasted waste agent and sieving the crushed waste agent with a 320-mesh sieve to obtain the raw material I.
Example 2
And roasting the FCC waste agent in an air atmosphere, wherein the roasting temperature is 500 and the roasting time is 10 hours. And crushing the roasted waste agent and sieving the crushed waste agent with a 280-mesh sieve to obtain a raw material II.
Example 3
And roasting the FCC waste agent in an air atmosphere at the roasting temperature of 600 ℃ for 4 h. And crushing the roasted waste agent and sieving the crushed waste agent with a 320-mesh sieve to obtain a raw material III.
Example 4
Taking 55kg of raw material I, 20kg of artificial kaliophilite, 2kg of graphite, 0.5kg of plant fiber, 16kg of 525 cement and 14kg of heavy magnesium oxide, mixing and ball-milling, adding water, kneading, granulating, and press-forming to obtain the raw ring a, curing for 24 hours by using water bubbles, wherein the crushing strength of the raw ring a after curing is 110N/particle. Sintering at 1250 +/-10 ℃ for 3 hours to obtain a pre-sintered carrier a, wherein the water absorption of the calcined carrier a is 21 percent, the pore volume of the carrier is 21.2mL/g and the pore-direction crushing strength is 225N/particle as measured by mercury intrusion method.
Dissolving nickel nitrate 110kg and lanthanum nitrate 12kg in water to prepare 100L solution, immersing the carrier a in the solution for 2 hours, taking out, drying at 100 ℃ for 4 hours, and decomposing at 450 ℃ for 2 hours. The catalyst A is prepared by repeating the steps of dipping, drying and decomposing once.
Example 5
Taking 55kg of raw material I, 20kg of artificial kaliophilite, 2kg of graphite, 0.5kg of plant fiber, 16kg of 625 cement and 14kg of heavy magnesium oxide, mixing and ball-milling, adding water, kneading, granulating, and press-forming to obtain the raw ring b, carrying out bubble curing for 24 hours, wherein the crushing strength of the raw ring b after curing is 92N/particle. Sintering at 1215 +/-15 ℃ for 3 hours to obtain a pre-sintered carrier b, wherein the water absorption of the calcined carrier b is 18.5 percent, the pore volume of the carrier is 18.9mL/g and the pore-direction crushing strength is 247N/particle as measured by mercury intrusion method.
Dissolving nickel nitrate 110kg and lanthanum nitrate 12kg in water to prepare 100L solution, immersing the carrier b in the solution for 2 hours, taking out, drying at 100 ℃ for 4 hours, and decomposing at 450 ℃ for 2 hours. The catalyst B is prepared by repeating the steps of dipping, drying and decomposing once.
Example 6
60kg of raw material II, 18kg of artificially synthesized kaliophilite, 2kg of graphite, 0.5kg of plant fiber, 18kg of 525 cement and 17kg of heavy magnesium oxide are mixed and ball-milled, kneaded by adding water, granulated and pressed to form to obtain the raw rings c, the raw rings c are cured for 36 hours by water soaking, and the crushing strength of the raw rings c after curing is 85N/particle. Sintering at 1285 +/-15 ℃ for 4 hours to obtain a pre-sintered carrier c, wherein the water absorption of the calcined carrier c is 19.9 percent, the pore volume of the carrier is 20.6mL/g as measured by mercury intrusion method, and the pore crushing strength is 234N/particle.
Dissolving 100L nickel nitrate and 10kg lanthanum nitrate in water to obtain 100L solution, soaking the carrier c in the solution for 2 hr, taking out, drying at 100 deg.C for 4 hr, and decomposing at 550 deg.C for 3 hr. The catalyst C is prepared by repeating the steps of dipping, drying and decomposing once.
Example 7
58kg of raw material III, 21kg of artificial kaliophilite, 2kg of graphite, 0.5kg of plant fiber, 18kg of 625 cement and 16kg of heavy magnesium oxide are mixed and ball-milled, kneaded by adding water, granulated and pressed to form to obtain the raw ring d, the raw ring d is cured for 36 hours by water soaking, and the crushing strength of the raw ring d after curing is 103N/particle. Sintering at 1275 +/-15 ℃ for 4 hours to obtain a pre-sintered carrier d, wherein the water absorption of the calcined carrier d is 20.7%, the pore volume of the carrier is 21.1mL/g, and the pore-direction crushing strength is 229N/particle as measured by mercury porosimetry.
Dissolving 100L nickel nitrate and 10kg lanthanum nitrate in water to obtain 100L solution, soaking the carrier d in the solution for 4 hr, taking out, drying at 100 deg.C for 4 hr, and decomposing at 550 deg.C for 3 hr. The catalyst D is prepared by repeating the steps of dipping, drying and decomposing once.
Example 8
Taking 20kg of raw materials I, II and III respectively, mixing and ball-milling 18kg of artificially synthesized kaliophilite, 2kg of graphite, 0.5kg of plant fiber, 17kg of 525 cement and 15kg of heavy magnesium oxide, adding water for kneading, granulating and pressing to form to obtain raw rings e, curing for 24 hours by using water bubbles, wherein the crushing strength of the raw rings e after curing is 109N/particle. Sintering at 1225 + -10 deg.C for 5 hr to obtain pre-sintered carrier e, which has water absorption of 21.9%, pore volume of 22.1mL/g, and pore crushing strength of 231N/particle as measured by mercury intrusion method.
Dissolving 120kg of nickel nitrate and 12kg of lanthanum nitrate in water to prepare 100L of solution, immersing the carrier e in the solution for 4 hours, taking out the carrier e, drying the carrier e for 4 hours at 100 ℃, and decomposing the carrier e for 4 hours at 500 ℃. The catalyst E is prepared by repeating the steps of dipping, drying and decomposing once.
Comparative example 1
Catalyst sample A, B, C, D, E, ZL 102451696, catalyst A from example 1, and commercial catalyst Z, were collected for characterization and evaluation.
Evaluation conditions were as follows:
no. six solvent oil.
Condition 1
The temperature of the whole bed layer is 700 ℃, the pressure is 0.5MPa, and H is2O/H210, hydrogen space velocity 400h-1The heat aging time was 50 hours.
Condition 2
Temperature: inlet 480 ℃ and outlet 700 ℃.
Pressure: 3.0 MPa.
H2/C：2.0。
Carbon space velocity: 10000h-1。
Reaction time: for 100 hours.
The evaluation results are shown in Table 1.
TABLE 1100 hours conversion Outlet evaluation results
Figure BDA0001368406720000061
Figure BDA0001368406720000071

Claims (7)

1. A gaseous hydrocarbon steam reforming upper stage catalyst characterized by: the catalyst takes nickel and rare earth as active components, the content of NiO in the catalyst is 5-25 wt.%, and the content of rare earth metal oxide is 0.3-15 wt.%; loading active components of nickel and rare earth on a carrier by adopting a co-impregnation method;
the carrier is prepared by the following method:
(1) FCC catalyst waste treatment:
roasting the FCC catalyst waste agent in an air atmosphere, crushing and sieving to obtain powder;
(2) preparing a carrier:
mixing powder, magnesium oxide, an anti-carbon auxiliary agent, a pore-forming agent, a lubricant and a binder, wherein the mixing mass ratio is 100: 25-200: 20-100: 1-5: 1-5: 30-120, then performing ball milling, kneading, granulating, extrusion forming to obtain a raw ring, and performing curing, drying and roasting to obtain a carrier;
in the step (1), the FCC catalyst waste agent is a catalyst waste agent prepared from ultrastable Y-type zeolite; the binder is pure clinker portland cement; the carbon-resistant auxiliary agent is artificially synthesized kaliophilite;
in the step (1), the roasting temperature is 500-700 ℃, and the roasting time is 2-10 h;
in the step (2), the roasting temperature is 1200-1300 ℃, and the roasting time is 2-6 hours.
2. The gaseous hydrocarbon steam reforming upper stage catalyst of claim 1, wherein: in the catalyst, the content of NiO is 8-17 wt.%, and the content of rare earth metal oxide is 0.5-12 wt.%.
3. The gaseous hydrocarbon steam reforming upper stage catalyst of claim 1, wherein: the pore volume of the carrier is 0.18-0.22 mL/g, and the pore crushing strength is more than 220N per particle.
4. The gaseous hydrocarbon steam reforming upper stage catalyst of claim 1, wherein: in the step (1), the sieving is carried out by a 280-320 mesh sieve.
5. The gaseous hydrocarbon steam reforming upper stage catalyst of claim 1, wherein: in the step (2), the curing is soaking in water for curing for 24-36 h.
6. The gaseous hydrocarbon steam reforming upper stage catalyst of claim 1, wherein: in the step (2), the crushing strength of the green ring after curing is more than 80N/particle.
7. A process for preparing the catalyst for steam reforming of gaseous hydrocarbon according to any one of claims 1 to 6, characterized in that: loading active components of nickel and rare earth on a carrier by adopting a co-impregnation method, wherein the impregnation time is 0.5-6 hours, decomposing at the temperature of 400-700 ℃ for 1-6 hours after drying, and then repeating impregnation, drying and decomposition once to obtain a catalyst finished product.
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1301666A (en) * 1999-12-29 2001-07-04 中国石化集团齐鲁石油化工公司 Steam preconversion catalyst for hydrocarbon
CN101543783A (en) * 2008-03-27 2009-09-30 中国石油化工股份有限公司 Suspension bed hydrocracking catalyst and preparation method and application thereof
CN102451696A (en) * 2010-10-22 2012-05-16 中国石油化工股份有限公司 Catalyst for reaction of hydrogen preparation or carbonyl synthesis gas preparation by hydrocarbon steam conversion
CN104549284A (en) * 2013-10-15 2015-04-29 中国石油化工股份有限公司 Gaseous hydrocarbon self-heating conversion catalyst and preparation method thereof
CN105561990A (en) * 2014-10-09 2016-05-11 中国石油化工股份有限公司 Hydrocarbon steam conversion catalyst and preparation method thereof

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1301666A (en) * 1999-12-29 2001-07-04 中国石化集团齐鲁石油化工公司 Steam preconversion catalyst for hydrocarbon
CN101543783A (en) * 2008-03-27 2009-09-30 中国石油化工股份有限公司 Suspension bed hydrocracking catalyst and preparation method and application thereof
CN102451696A (en) * 2010-10-22 2012-05-16 中国石油化工股份有限公司 Catalyst for reaction of hydrogen preparation or carbonyl synthesis gas preparation by hydrocarbon steam conversion
CN104549284A (en) * 2013-10-15 2015-04-29 中国石油化工股份有限公司 Gaseous hydrocarbon self-heating conversion catalyst and preparation method thereof
CN105561990A (en) * 2014-10-09 2016-05-11 中国石油化工股份有限公司 Hydrocarbon steam conversion catalyst and preparation method thereof

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